Dual activator-support catalyst systems

ABSTRACT

Disclosed herein are polymerization processes for the production of olefin polymers. These polymerization processes use a catalyst system containing at least two activator-supports. One activator-support is a halided solid oxide, and the other activator-support is a sulfated solid oxide and/or phosphated solid oxide.

BACKGROUND OF THE INVENTION

Polyolefins such as high density polyethylene (HDPE) homopolymer and linear low density polyethylene (LLDPE) copolymer can be produced using various combinations of catalyst systems and polymerization processes. Metallocene-based catalysts systems, for example, typically contain a metallocene compound and an activator. It is well established that the structure of the metallocene compound can impact the polymerization process and the resulting polymer properties, including molecular weight parameters such as weight-average molecular weight (Mw), number-average molecular weight (Mn), and molecular weight distribution (MWD). In contrast, the present invention is directed generally to the impact of the activator on the polymerization process and the resulting polymer properties, for example, the Mw and Mn of the polymer.

SUMMARY OF THE INVENTION

This summary is provided to introduce a selection of concepts in a simplified form that are further described below in the detailed description. This summary is not intended to identify required or essential features of the claimed subject matter. Nor is this summary intended to be used to limit the scope of the claimed subject matter.

The present invention generally relates to new catalyst compositions, methods for preparing catalyst compositions, methods for using the catalyst compositions to polymerize olefins, the polymer resins produced using such catalyst compositions, and articles produced using these polymer resins. In particular, aspects of the present invention are directed to catalyst compositions employing two activator-support components. Activator-support component I can comprise a halided solid oxide, while activator-support component II can comprise a sulfated solid oxide and/or a phosphated solid oxide. In one aspect, a catalyst composition is disclosed which can comprise a metallocene compound, activator-support I, and activator-support II. Optionally, this catalyst composition can further comprise a co-catalyst. Such catalyst compositions can be used to produce, for example, ethylene-based homopolymers and copolymers.

The present invention also contemplates and encompasses olefin polymerization processes. Such processes can comprise contacting a catalyst composition with an olefin monomer and optionally an olefin comonomer in a polymerization reactor system under polymerization conditions to produce an olefin polymer. Generally, the catalyst composition employed can comprise any of the metallocene compounds, any of the activator-support I materials, any of the activator-support II materials, and any of the optional co-catalysts disclosed herein. For example, organoaluminum compounds can be utilized in the catalyst compositions and/or polymerization processes.

In a particular aspect of this invention, an olefin polymerization process can comprise contacting a catalyst composition described herein (i.e., with activator-support I and activator-support II) with an olefin monomer and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce an olefin polymer. In this aspect, a molecular weight parameter—for instance, number-average molecular weight (Mn), weight-average molecular weight (Mw), etc.—of the olefin polymer produced by the process can be greater than the molecular weight parameter of an olefin polymer obtained under the same polymerization conditions without activator-support I in the catalyst composition, as well as greater than the molecular weight parameter of an olefin polymer obtained under the same polymerization conditions without activator-support II in the catalyst composition. Unexpectedly, the polymerization process employing a catalyst system containing activator-support I and activator-support II can produce olefin polymers having higher molecular weights than polymers produced under the same polymerization conditions, but with catalyst systems containing only activator-support I or only activator-support II.

Polymers produced from the polymerization of olefins, resulting in homopolymers, copolymers, terpolymers, etc., can be used to produce various articles of manufacture. A representative and non-limiting example of an olefin polymer (e.g., an ethylene copolymer) consistent with aspects of this invention can be characterized as having the following properties: a melt index of less than or equal to about 25 g/10 min, a density in a range from about 0.89 g/cm³ to about 0.96 g/cm³, a Mw in a range from about 75,000 to about 500,000 g/mol, and a Mn in a range from about 5,000 to about 150,000 g/mol.

Both the foregoing summary and the following detailed description provide examples and are explanatory only. Accordingly, the foregoing summary and the following detailed description should not be considered to be restrictive. Further, features or variations may be provided in addition to those set forth herein. For example, certain aspects and embodiments may be directed to various feature combinations and sub-combinations described in the detailed description.

DEFINITIONS

To define more clearly the terms used herein, the following definitions are provided. Unless otherwise indicated, the following definitions are applicable to this disclosure. If a term is used in this disclosure but is not specifically defined herein, the definition from the IUPAC Compendium of Chemical Terminology, 2nd Ed (1997), can be applied, as long as that definition does not conflict with any other disclosure or definition applied herein, or render indefinite or non-enabled any claim to which that definition is applied. To the extent that any definition or usage provided by any document incorporated herein by reference conflicts with the definition or usage provided herein, the definition or usage provided herein controls.

Regarding claim transitional terms or phrases, the transitional term “comprising,” which is synonymous with “including,” “containing,” or “characterized by,” is open-ended and does not exclude additional, unrecited elements or method steps. The transitional phrase “consisting of” excludes any element, step, or ingredient not specified in the claim. The transitional phrase “consisting essentially of” limits the scope of a claim to the specified components or steps and those that do not materially affect the basic and novel characteristic(s) of the claimed invention. A “consisting essentially of” claim occupies a middle ground between closed claims that are written in a “consisting of” format and fully open claims that are drafted in a “comprising” format. For example, a composition consisting essentially of component A can include impurities typically present in a commercially produced or commercially available sample of component A. When a claim includes different features and/or feature classes (for example, a method step, composition features, among other possibilities), the transitional terms comprising, consisting essentially of, and consisting of, apply only to the feature class to which it is utilized, and it is possible to have different transitional terms or phrases utilized with different features within a claim. For example, a method can consist of certain steps, but utilize a catalyst system comprising recited components and other non-recited components. While compositions and methods are described herein in terms of “comprising” various components or steps, the compositions and methods can also “consist essentially of” or “consist of” the various components or steps, unless stated otherwise. For example, a catalyst composition consistent with aspects of the present invention can comprise; alternatively, can consist essentially of; or alternatively, can consist of; (i) activator-support I, (ii) activator-support II, (iii) a metallocene compound, and (iv) optionally, a co-catalyst.

The terms “a,” “an,” “the,” etc., are intended to include plural alternatives, e.g., at least one, unless otherwise specified. For instance, the disclosure of “a co-catalyst” or “a metallocene compound” is meant to encompass one, or mixtures or combinations of more than one, co-catalyst or metallocene compound, respectively, unless otherwise specified.

Generally, groups of elements are indicated using the numbering scheme indicated in the version of the periodic table of elements published in Chemical and Engineering News, 63(5), 27, 1985. In some instances, a group of elements can be indicated using a common name assigned to the group; for example, alkali metals for Group 1 elements, alkaline earth metals for Group 2 elements, transition metals for Group 3-12 elements, and halogens or halides for Group 17 elements.

For any particular compound disclosed herein, the general structure or name presented is also intended to encompass all structural isomers, conformational isomers, and stereoisomers that can arise from a particular set of substituents, unless indicated otherwise. Thus, a general reference to a compound includes all structural isomers unless explicitly indicated otherwise; e.g., a general reference to pentane includes n-pentane, 2-methyl-butane, and 2,2-dimethylpropane, while a general reference to a butyl group includes an n-butyl group, a sec-butyl group, an iso-butyl group, and a tert-butyl group. Additionally, the reference to a general structure or name encompasses all enantiomers, diastereomers, and other optical isomers whether in enantiomeric or racemic forms, as well as mixtures of stereoisomers, as the context permits or requires. For any particular formula or name that is presented, any general formula or name presented also encompasses all conformational isomers, regioisomers, and stereoisomers that can arise from a particular set of substituents.

A chemical “group” is described according to how that group is formally derived from a reference or “parent” compound, for example, by the number of hydrogen atoms formally removed from the parent compound to generate the group, even if that group is not literally synthesized in this manner. These groups can be utilized as substituents or coordinated or bonded to metal atoms. By way of example, an “alkyl group” formally can be derived by removing one hydrogen atom from an alkane, while an “alkylene group” formally can be derived by removing two hydrogen atoms from an alkane. Moreover, a more general term can be used to encompass a variety of groups that formally are derived by removing any number (“one or more”) of hydrogen atoms from a parent compound, which in this example can be described as an “alkane group,” and which encompasses an “alkyl group,” an “alkylene group,” and materials have three or more hydrogen atoms, as necessary for the situation, removed from the alkane. The disclosure that a substituent, ligand, or other chemical moiety can constitute a particular “group” implies that the well-known rules of chemical structure and bonding are followed when that group is employed as described. When describing a group as being “derived by,” “derived from,” “formed by,” or “formed from,” such terms are used in a formal sense and are not intended to reflect any specific synthetic method or procedure, unless specified otherwise or the context requires otherwise.

The term “substituted” when used to describe a group, for example, when referring to a substituted analog of a particular group, is intended to describe any non-hydrogen moiety that formally replaces a hydrogen in that group, and is intended to be non-limiting. A group or groups can also be referred to herein as “unsubstituted” or by equivalent terms such as “non-substituted,” which refers to the original group in which a non-hydrogen moiety does not replace a hydrogen within that group. Unless otherwise specified, “substituted” is intended to be non-limiting and include inorganic substituents or organic substituents as understood by one of ordinary skill in the art.

The term “hydrocarbon” whenever used in this specification and claims refers to a compound containing only carbon and hydrogen. Other identifiers can be utilized to indicate the presence of particular groups in the hydrocarbon (e.g., halogenated hydrocarbon indicates that the presence of one or more halogen atoms replacing an equivalent number of hydrogen atoms in the hydrocarbon). The term “hydrocarbyl group” is used herein in accordance with the definition specified by IUPAC: a univalent group formed by removing a hydrogen atom from a hydrocarbon (that is, a group containing only carbon and hydrogen). Non-limiting examples of hydrocarbyl groups include ethyl, phenyl, tolyl, propenyl, and the like. Similarly, a “hydrocarbylene group” refers to a group formed by removing two hydrogen atoms from a hydrocarbon, either two hydrogen atoms from one carbon atom or one hydrogen atom from each of two different carbon atoms. Therefore, in accordance with the terminology used herein, a “hydrocarbon group” refers to a generalized group formed by removing one or more hydrogen atoms (as necessary for the particular group) from a hydrocarbon. A “hydrocarbyl group,” “hydrocarbylene group,” and “hydrocarbon group” can be aliphatic or aromatic, acyclic or cyclic, and/or linear or branched. A “hydrocarbyl group,” “hydrocarbylene group,” and “hydrocarbon group” can include rings, ring systems, aromatic rings, and aromatic ring systems, which contain only carbon and hydrogen. “Hydrocarbyl groups,” “hydrocarbylene groups,” and “hydrocarbon groups” include, by way of example, aryl, arylene, arene groups, alkyl, alkylene, alkane groups, cycloalkyl, cycloalkylene, cycloalkane groups, aralkyl, aralkylene, and aralkane groups, respectively, among other groups as members.

An aliphatic compound is a class of acyclic or cyclic, saturated or unsaturated, carbon compounds, excluding aromatic compounds, e.g., an aliphatic compound is a non-aromatic organic compound. An “aliphatic group” is a generalized group formed by removing one or more hydrogen atoms (as necessary for the particular group) from a carbon atom of an aliphatic compound. Aliphatic compounds and therefore aliphatic groups can contain organic functional group(s) and/or atom(s) other than carbon and hydrogen.

The term “alkane” whenever used in this specification and claims refers to a saturated hydrocarbon compound. Other identifiers can be utilized to indicate the presence of particular groups in the alkane (e.g., halogenated alkane indicates that the presence of one or more halogen atoms replacing an equivalent number of hydrogen atoms in the alkane). The term “alkyl group” is used herein in accordance with the definition specified by IUPAC: a univalent group formed by removing a hydrogen atom from an alkane. Similarly, an “alkylene group” refers to a group formed by removing two hydrogen atoms from an alkane (either two hydrogen atoms from one carbon atom or one hydrogen atom from two different carbon atoms). An “alkane group” is a general term that refers to a group formed by removing one or more hydrogen atoms (as necessary for the particular group) from an alkane. An “alkyl group,” “alkylene group,” and “alkane group” can be acyclic or cyclic and/or linear or branched unless otherwise specified.

A cycloalkane is a saturated cyclic hydrocarbon, with or without side chains, for example, cyclobutane. Other identifiers can be utilized to indicate the presence of particular groups in the cycloalkane (e.g., halogenated cycloalkane indicates that the presence of one or more halogen atoms replacing an equivalent number of hydrogen atoms in the cycloalkane). Unsaturated cyclic hydrocarbons having one endocyclic double or one triple bond are called cycloalkenes and cycloalkynes, respectively. Those having more than one such multiple bond are cycloalkadienes, cycloalkatrienes, and so forth. Other identifiers can be utilized to indicate the presence of particular groups in the cycloalkenes, cycloalkadienes, cycloalkatrienes, and so forth.

A “cycloalkyl group” is a univalent group derived by removing a hydrogen atom from a ring carbon atom of a cycloalkane. For example, a 1-methylcyclopropyl group and a 2-methylcyclopropyl group are illustrated as follows.

Similarly, a “cycloalkylene group” refers to a group derived by removing two hydrogen atoms from a cycloalkane, at least one of which is a ring carbon. Thus, a “cycloalkylene group” includes a group derived from a cycloalkane in which two hydrogen atoms are formally removed from the same ring carbon, a group derived from a cycloalkane in which two hydrogen atoms are formally removed from two different ring carbons, and a group derived from a cycloalkane in which a first hydrogen atom is formally removed from a ring carbon and a second hydrogen atom is formally removed from a carbon atom that is not a ring carbon. A “cycloalkane group” refers to a generalized group formed by removing one or more hydrogen atoms (as necessary for the particular group and at least one of which is a ring carbon) from a cycloalkane.

The term “alkene” whenever used in this specification and claims refers a linear or branched hydrocarbon olefin that has one carbon-carbon double bond and the general formula C_(n)H_(2n). Alkadienes refer to a linear or branched hydrocarbon olefin having two carbon-carbon double bonds and the general formula C_(n)H_(2n-2), and alkatrienes refer to linear or branched hydrocarbon olefins having three carbon-carbon and the general formula C_(n)H_(2n-4). Alkenes, alkadienes, and alkatrienes can be further identified by the position of the carbon-carbon double bond(s). Other identifiers can be utilized to indicate the presence or absence of particular groups within an alkene, alkadiene, or alkatriene. For example, a haloalkene refers to an alkene having one or more hydrogen atoms replace with a halogen atom.

An “alkenyl group” is a univalent group derived from an alkene by removal of a hydrogen atom from any carbon atom of the alkene. Thus, “alkenyl group” includes groups in which the hydrogen atom is formally removed from an sp² hybridized (olefinic) carbon atom and groups in which the hydrogen atom is formally removed from any other carbon atom. For example and unless otherwise specified, 1-propenyl (—CH═CHCH₃), 2-propenyl (—CH₂CH═CH₂), and 3-butenyl (—CH₂CH₂CH═CH₂) groups are encompassed with the term “alkenyl group.” Similarly, an “alkenylene group” refers to a group formed by formally removing two hydrogen atoms from an alkene, either two hydrogen atoms from one carbon atom or one hydrogen atom from two different carbon atoms. An “alkene group” refers to a generalized group formed by removing one or more hydrogen atoms (as necessary for the particular group) from an alkene. When the hydrogen atom is removed from a carbon atom participating in a carbon-carbon double bond, the regiochemistry of the carbon from which the hydrogen atom is removed, and regiochemistry of the carbon-carbon double bond can both be specified. Other identifiers can be utilized to indicate the presence or absence of particular groups within an alkene group. Alkene groups can also be further identified by the position of the carbon-carbon double bond.

An arene is an aromatic hydrocarbon, with or without side chains (e.g., benzene, toluene, or xylene, among others). An “aryl group” is a group derived from the formal removal of a hydrogen atom from an aromatic ring carbon of an arene. It should be noted that the arene can contain a single aromatic hydrocarbon ring (e.g., benzene or toluene), contain fused aromatic rings (e.g., naphthalene or anthracene), and contain one or more isolated aromatic rings covalently linked via a bond (e.g., biphenyl) or non-aromatic hydrocarbon group(s) (e.g., diphenylmethane). One example of an “aryl group” is ortho-tolyl (o-tolyl), the structure of which is shown here.

An “aralkyl group” is an aryl-substituted alkyl group having a free valance at a non-aromatic carbon atom, for example, a benzyl group, or a 2-phenyleth-1yl group, among others.

A “halide” has its usual meaning. Examples of halides include fluoride, chloride, bromide, and iodide.

The term “polymer” is used herein generically to include olefin homopolymers, copolymers, terpolymers, and so forth. A copolymer is derived from an olefin monomer and one olefin comonomer, while a terpolymer is derived from an olefin monomer and two olefin comonomers. Accordingly, “polymer” encompasses copolymers, terpolymers, etc., derived from any olefin monomer and comonomer(s) disclosed herein. Similarly, an ethylene polymer would include ethylene homopolymers, ethylene copolymers, ethylene terpolymers, and the like. As an example, an olefin copolymer, such as an ethylene copolymer, can be derived from ethylene and a comonomer, such as 1-butene, 1-hexene, or 1-octene. If the monomer and comonomer were ethylene and 1-hexene, respectively, the resulting polymer could be categorized an as ethylene/1-hexene copolymer.

In like manner, the scope of the term “polymerization” includes homopolymerization, copolymerization, terpolymerization, etc. Therefore, a copolymerization process could involve contacting one olefin monomer (e.g., ethylene) and one olefin comonomer (e.g., 1-hexene) to produce a copolymer.

The term “co-catalyst” is used generally herein to refer to compounds such as aluminoxane compounds, organoboron or organoborate compounds, ionizing ionic compounds, organoaluminum compounds, organozinc compounds, organomagnesium compounds, organolithium compounds, and the like, that can constitute one component of a catalyst composition, when used, for example, in addition to an activator-support. The term “co-catalyst” is used regardless of the actual function of the compound or any chemical mechanism by which the compound may operate.

The terms “activator-support,” “chemically-treated solid oxide,” “treated solid oxide compound,” and the like, are used herein to indicate a solid, inorganic oxide of relatively high porosity, which can exhibit Lewis acidic or Brønsted acidic behavior, and which has been treated with an electron-withdrawing component, typically an anion, and which is calcined. The electron-withdrawing component is typically an electron-withdrawing anion source compound. Thus, the chemically-treated solid oxide can comprise a calcined contact product of at least one solid oxide with at least one electron-withdrawing anion source compound. Typically, the chemically-treated solid oxide comprises at least one acidic solid oxide compound. The term “activator-support” is not used to imply these activator-support components are inert, and such components should not be construed as an inert component of a catalyst composition. The term “activator,” as used herein, refers generally to a substance that is capable of converting a metallocene component into a catalyst that can polymerize olefins, or converting a contact product of a metallocene component and a component that provides an activatable ligand (e.g., an alkyl, a hydride) to the metallocene, when the metallocene compound does not already comprise such a ligand, into a catalyst that can polymerize olefins. This term is used regardless of the actual activating mechanism. Illustrative activators include activator-supports or chemically-treated solid oxides.

The term “fluoroorgano boron compound” is used herein with its ordinary meaning to refer to neutral compounds of the form BY₃. The term “fluoroorgano borate compound” also has its usual meaning to refer to the monoanionic salts of a fluoroorgano boron compound of the form [cation]⁺[BY₄]⁻, where Y represents a fluorinated organic group. Materials of these types are generally and collectively referred to as “organoboron or organoborate compounds.”

The term “metallocene” as used herein, describe compounds comprising at least one η³ to η⁵-cycloalkadienyl-type moiety, wherein η³ to η⁵-cycloalkadienyl moieties include cyclopentadienyl ligands, indenyl ligands, fluorenyl ligands, and the like, including partially saturated or substituted derivatives or analogs of any of these. Possible substituents on these ligands may include H, therefore this invention comprises ligands such as tetrahydroindenyl, tetrahydrofluorenyl, octahydrofluorenyl, partially saturated indenyl, partially saturated fluorenyl, substituted partially saturated indenyl, substituted partially saturated fluorenyl, and the like. In some contexts, the metallocene can be referred to simply as the “catalyst,” in much the same way the term “co-catalyst” can be used herein to refer to, for example, an organoaluminum compound.

The terms “catalyst composition,” “catalyst mixture,” “catalyst system,” and the like, do not depend upon the actual product or composition resulting from the contact or reaction of the initial components of the claimed catalyst composition/mixture/system, the nature of the active catalytic site, or the fate of the co-catalyst, the metallocene compound, any olefin monomer used to prepare a precontacted mixture, or the activator-supports, after combining these components. Therefore, the terms “catalyst composition,” “catalyst mixture,” “catalyst system,” and the like, encompass the initial starting components of the composition, as well as whatever product(s) may result from contacting these initial starting components, and this is inclusive of both heterogeneous and homogenous catalyst systems or compositions. The terms “catalyst composition,” “catalyst mixture,” “catalyst system,” and the like, can be used interchangeably throughout this disclosure.

The term “contact product” is used herein to describe compositions wherein the components are contacted together in any order, in any manner, and for any length of time. For example, the components can be contacted by blending or mixing. Further, contacting of any component can occur in the presence or absence of any other component of the compositions described herein. Combining additional materials or components can be done by any suitable method. Further, the term “contact product” includes mixtures, blends, solutions, slurries, reaction products, and the like, or combinations thereof. Although “contact product” can include reaction products, it is not required for the respective components to react with one another. Similarly, the term “contacting” is used herein to refer to materials which can be blended, mixed, slurried, dissolved, reacted, treated, or otherwise contacted in some other manner.

The term “precontacted” mixture is used herein to describe a first mixture of catalyst components that are contacted for a first period of time prior to the first mixture being used to form a “postcontacted” or second mixture of catalyst components that are contacted for a second period of time. Typically, the precontacted mixture can describe a mixture of a metallocene compound (one or more than one), olefin monomer (or monomers), and organoaluminum compound (or compounds), before this mixture is contacted with an activator-support(s) and optional additional organoaluminum compound. Thus, precontacted describes components that are used to contact each other, but prior to contacting the components in the second, postcontacted mixture. Accordingly, this invention can occasionally distinguish between a component used to prepare the precontacted mixture and that component after the mixture has been prepared. For example, according to this description, it is possible for the precontacted organoaluminum compound, once it is contacted with the metallocene compound and the olefin monomer, to have reacted to form at least one chemical compound, formulation, or structure different from the distinct organoaluminum compound used to prepare the precontacted mixture. In this case, the precontacted organoaluminum compound or component is described as comprising an organoaluminum compound that was used to prepare the precontacted mixture.

Additionally, the precontacted mixture can describe a mixture of metallocene compound(s) and organoaluminum compound(s), prior to contacting this mixture with an activator-support(s). This precontacted mixture also can describe a mixture of metallocene compound(s), olefin monomer(s), and activator-support(s), before this mixture is contacted with an organoaluminum co-catalyst compound or compounds.

Similarly, the term “postcontacted” mixture is used herein to describe a second mixture of catalyst components that are contacted for a second period of time, and one constituent of which is the “precontacted” or first mixture of catalyst components that were contacted for a first period of time. Typically, the term “postcontacted” mixture is used herein to describe the mixture of metallocene compound(s), olefin monomer(s), organoaluminum compound(s), and activator-support(s) formed from contacting the precontacted mixture of a portion of these components with any additional components added to make up the postcontacted mixture.

Although any methods, devices, and materials similar or equivalent to those described herein can be used in the practice or testing of the invention, the typical methods, devices and materials are herein described.

All publications and patents mentioned herein are incorporated herein by reference for the purpose of describing and disclosing, for example, the constructs and methodologies that are described in the publications, which might be used in connection with the presently described invention. The publications discussed throughout the text are provided solely for their disclosure prior to the filing date of the present application. Nothing herein is to be construed as an admission that the inventors are not entitled to antedate such disclosure by virtue of prior invention.

Applicants disclose several types of ranges in the present invention. When Applicants disclose or claim a range of any type, Applicants' intent is to disclose or claim individually each possible number that such a range could reasonably encompass, including end points of the range as well as any sub-ranges and combinations of sub-ranges encompassed therein. For example, when the Applicants disclose or claim a chemical moiety having a certain number of carbon atoms, Applicants' intent is to disclose or claim individually every possible number that such a range could encompass, consistent with the disclosure herein. For example, the disclosure that a moiety is a C₁ to C₁₈ hydrocarbyl group, or in alternative language, a hydrocarbyl group having from 1 to 18 carbon atoms, as used herein, refers to a moiety that can be selected independently from a hydrocarbyl group having 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, or 18 carbon atoms, as well as any range between these two numbers (for example, a C₁ to C₈ hydrocarbyl group), and also including any combination of ranges between these two numbers (for example, a C₂ to C₄ and a C₁₂ to C₁₆ hydrocarbyl group).

Similarly, another representative example follows for the number-average molecular weight (Mn) of an olefin polymer produced in an aspect of this invention. By a disclosure that the Mn can be in a range from about 10,000 to about 50,000 g/mol, Applicants intend to recite that the Mn can be equal to about 10,000, about 15,000, about 20,000, about 25,000, about 30,000, about 35,000, about 40,000, about 45,000, or about 50,000 g/mol. Additionally, the Mn can be within any range from about 10,000 to about 50,000 (for example, from about 10,000 to about 25,000), and this also includes any combination of ranges between about 10,000 and about 50,000 (for example, the Mn can be in a range from about 10,000 to about 20,000, or from about 25,000 to about 45,000). Likewise, all other ranges disclosed herein should be interpreted in a manner similar to these two examples.

Applicants reserve the right to proviso out or exclude any individual members of any such group, including any sub-ranges or combinations of sub-ranges within the group, that can be claimed according to a range or in any similar manner, if for any reason Applicants choose to claim less than the full measure of the disclosure, for example, to account for a reference that Applicants may be unaware of at the time of the filing of the application. Further, Applicants reserve the right to proviso out or exclude any individual substituents, analogs, compounds, ligands, structures, or groups thereof, or any members of a claimed group, if for any reason Applicants choose to claim less than the full measure of the disclosure, for example, to account for a reference that Applicants may be unaware of at the time of the filing of the application.

DETAILED DESCRIPTION OF THE INVENTION

The present invention is directed generally to new catalyst compositions, methods for preparing catalyst compositions, methods for using the catalyst compositions to polymerize olefins, the polymer resins produced using such catalyst compositions, and articles produced using these polymer resins. In particular, the present invention relates to catalyst compositions containing two activator-support components and to polymerization processes utilizing such catalyst compositions.

Metallocene Compounds

In some aspects, the catalyst system can comprise activator-support I, activator-support II, and a metallocene compound (one or more than one). Generally, the metallocene compound can comprise, for example, a transition metal (one or more than one) from Groups IIIB-VIIIB of the Periodic Table of the Elements. In one aspect, the metallocene compound can comprise a Group III, IV, V, or VI transition metal, or a combination of two or more transition metals. The metallocene compound can comprise chromium, titanium, zirconium, hafnium, vanadium, or a combination thereof, or can comprise titanium, zirconium, hafnium, or a combination thereof, in certain aspects. Accordingly, the metallocene compound can comprise titanium, or zirconium, or hafnium, either singly or in combination.

While not being limited thereto, the metallocene compound can comprise an unbridged metallocene compound in an aspect of this invention. For instance, the metallocene compound can comprise an unbridged zirconium or hafnium based metallocene compound and/or an unbridged zirconium and/or hafnium based dinuclear metallocene compound. In one aspect, the metallocene compound can comprise an unbridged zirconium or hafnium based metallocene compound containing two cyclopentadienyl groups, two indenyl groups, or a cyclopentadienyl and an indenyl group. In another aspect, the metallocene compound can comprise an unbridged zirconium based metallocene compound containing two cyclopentadienyl groups, two indenyl groups, or a cyclopentadienyl and an indenyl group. Illustrative and non-limiting examples of unbridged metallocene compounds (e.g., with zirconium or hafnium) that can be employed in catalyst systems consistent with aspects of the present invention are described in U.S. Pat. Nos. 7,226,886 and 7,619,047, the disclosures of which are incorporated herein by reference in their entirety.

In other aspects, the metallocene compound can comprise an unbridged zirconium and/or hafnium based dinuclear metallocene compound. For example, the metallocene compound can comprise an unbridged zirconium based homodinuclear metallocene compound, or an unbridged hafnium based homodinuclear metallocene compound, or an unbridged zirconium and/or hafnium based heterodinuclear metallocene compound (i.e., a dinuclear compound with two hafniums, or two zirconiums, or one zirconium and one hafnium). These and other suitable dinuclear compounds (bridged and unbridged) are described in U.S. Pat. Nos. 7,863,210, 7,919,639, 8,012,900, and 8,080,681, the disclosures of which are incorporated herein by reference in their entirety.

The metallocene compound can comprise a bridged metallocene compound, e.g., with titanium, zirconium, or hafnium. Accordingly, the metallocene compound can comprise a bridged zirconium based metallocene compound with a fluorenyl group, and with no aryl groups on the bridging group, or a bridged zirconium based metallocene compound with a cyclopentadienyl group and a fluorenyl group, and with no aryl groups on the bridging group. Such bridged metallocenes, in some aspects, can contain an alkenyl substituent (e.g., a terminal alkenyl) on the bridging group and/or on a cyclopentadienyl-type group (e.g., a cyclopentadienyl group, a fluorenyl group, etc.).

In another aspect, the metallocene compound can comprise a bridged zirconium or hafnium based metallocene compound with a fluorenyl group, and an aryl group on the bridging group. Thus, the metallocene compound can comprise a bridged zirconium or hafnium based metallocene compound with a cyclopentadienyl group and fluorenyl group, and an aryl group on the bridging group; alternatively, a bridged zirconium based metallocene compound with a fluorenyl group, and an aryl group on the bridging group; or alternatively, a bridged hafnium based metallocene compound with a fluorenyl group, and an aryl group on the bridging group. In these and other aspects, the aryl group on the bridging group can be a phenyl group. Optionally, these bridged metallocenes can contain an alkenyl substituent (e.g., a terminal alkenyl) on the bridging group and/or on a cyclopentadienyl-type group.

Illustrative and non-limiting examples of bridged metallocene compounds (e.g., with zirconium or hafnium) that can be employed in catalyst systems consistent with aspects of the present invention are described in U.S. Pat. Nos. 7,041,617, 7,226,886, 7,517,939, and 7,619,047, the disclosures of which are incorporated herein by reference in their entirety.

In one aspect, the catalyst composition contains only one metallocene compound, while in another aspect, the catalyst composition contains two or more metallocene compounds. If two or more metallocene compounds are used, the relative amounts of each respective metallocene compound are not restricted to any particular range. For instance, if the catalyst composition contains two metallocene compounds, the weight ratio of the first metallocene catalyst component to the second metallocene catalyst component can be in a range of from about 1:100 to about 100:1, from about 1:50 to about 50:1, from about 1:20 to about 20:1, from about 1:10 to about 10:1, or from about 1:5 to about 5:1. Accordingly, suitable ranges for the weight ratio of the first metallocene catalyst component to the second metallocene catalyst component can include, but are not limited to, from about 1:4 to about 4:1, from about 1:3 to about 3:1, from about 1:2 to about 2:1, from about 1:1.5 to about 1.5:1, from about 1:1.25 to about 1.25:1, or from about 1:1.1 to about 1.1:1, and the like.

Activator-Supports

The present invention encompasses various catalyst compositions containing activator-supports, often referred to as chemically-treated solid oxides. Generally, chemically-treated solid oxides exhibit enhanced acidity as compared to the corresponding untreated solid oxide compound. The chemically-treated solid oxide also can function as a catalyst activator as compared to the corresponding untreated solid oxide. While the chemically-treated solid oxide can activate a metallocene complex in the absence of co-catalysts, it is not necessary to eliminate co-catalysts from the catalyst composition. The activation function of the activator-support can enhance the activity of catalyst composition as a whole, as compared to a catalyst composition containing the corresponding untreated solid oxide. However, it is believed that the chemically-treated solid oxide can function as an activator, even in the absence of organoaluminum compounds, aluminoxanes, organoboron or organoborate compounds, ionizing ionic compounds, and the like.

The chemically-treated solid oxide can comprise a solid oxide treated with an electron-withdrawing anion. While not intending to be bound by the following statement, it is believed that treatment of the solid oxide with an electron-withdrawing component augments or enhances the acidity of the oxide. Thus, either the activator-support exhibits Lewis or Brønsted acidity that is typically greater than the Lewis or Brønsted acid strength of the untreated solid oxide, or the activator-support has a greater number of acid sites than the untreated solid oxide, or both. One method to quantify the acidity of the chemically-treated and untreated solid oxide materials can be by comparing the polymerization activities of the treated and untreated oxides under acid catalyzed reactions.

Chemically-treated solid oxides of this invention generally can be formed from an inorganic solid oxide that exhibits Lewis acidic or Brønsted acidic behavior and has a relatively high porosity. The solid oxide can be chemically-treated with an electron-withdrawing component, typically an electron-withdrawing anion, to form an activator-support.

According to one aspect of the present invention, the solid oxide used to prepare the chemically-treated solid oxide can have a pore volume greater than about 0.1 cc/g. According to another aspect of the present invention, the solid oxide can have a pore volume greater than about 0.5 cc/g. According to yet another aspect of the present invention, the solid oxide can have a pore volume greater than about 1.0 cc/g.

In another aspect, the solid oxide can have a surface area of from about 100 to about 1000 m²/g. In yet another aspect, the solid oxide can have a surface area of from about 200 to about 800 m²/g. In still another aspect of the present invention, the solid oxide can have a surface area of from about 250 to about 600 m²/g.

The chemically-treated solid oxide can comprise a solid inorganic oxide comprising oxygen and one or more elements selected from Group 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, or 15 of the periodic table, or comprising oxygen and one or more elements selected from the lanthanide or actinide elements (See: Hawley's Condensed Chemical Dictionary, 11^(th) Ed., John Wiley & Sons, 1995; Cotton, F. A., Wilkinson, G., Murillo, C. A., and Bochmann, M., Advanced Inorganic Chemistry, 6^(th) Ed., Wiley-Interscience, 1999). For example, the inorganic oxide can comprise oxygen and an element, or elements, selected from Al, B, Be, Bi, Cd, Co, Cr, Cu, Fe, Ga, La, Mn, Mo, Ni, Sb, Si, Sn, Sr, Th, Ti, V, W, P, Y, Zn, and Zr.

Suitable examples of solid oxide materials or compounds that can be used to form the chemically-treated solid oxide can include, but are not limited to, Al₂O₃, B₂O₃, BeO, Bi₂O₃, CdO, Co₃O₄, Cr₂O₃, CuO, Fe₂O₃, Ga₂O₃, La₂O₃, Mn₂O₃, MoO₃, NiO, P₂O₅, Sb₂O₅, SiO₂, SnO₂, SrO, ThO₂, TiO₂, V₂O₅, WO₃, Y₂O₃, ZnO, ZrO₂, and the like, including mixed oxides thereof, and combinations thereof. For example, the solid oxide can comprise silica, alumina, silica-alumina, silica-coated alumina, aluminum phosphate, aluminophosphate, heteropolytungstate, titania, zirconia, magnesia, boria, zinc oxide, mixed oxides thereof, or any combination thereof.

The solid oxide of this invention encompasses oxide materials such as alumina, “mixed oxides” thereof such as silica-alumina, materials where one oxide is coated with another, as well as any combinations and mixtures thereof. The mixed oxide compounds such as silica-alumina can be single or multiple chemical phases with more than one metal combined with oxygen to form a solid oxide compound. Examples of mixed oxides that can be used in the activator-support of the present invention, either singly or in combination, can include, but are not limited to, silica-alumina, silica-titania, silica-zirconia, zeolites, various clay minerals, alumina-titania, alumina-zirconia, zinc-aluminate, alumina-boria, silica-boria, aluminophosphate-silica, titania-zirconia, and the like. The solid oxide of this invention also encompasses oxide materials such as silica-coated alumina, as described in U.S. Pat. No. 7,884,163, the disclosure of which is incorporated herein by reference in its entirety.

The electron-withdrawing component used to treat the solid oxide can be any component that increases the Lewis or Brønsted acidity of the solid oxide upon treatment (as compared to the solid oxide that is not treated with at least one electron-withdrawing anion). According to one aspect of the present invention, the electron-withdrawing component can be an electron-withdrawing anion derived from a salt, an acid, or other compound, such as a volatile organic compound, that serves as a source or precursor for that anion. Examples of electron-withdrawing anions can include, but are not limited to, sulfate, bisulfate, fluoride, chloride, bromide, iodide, fluorosulfate, fluoroborate, phosphate, fluorophosphate, trifluoroacetate, triflate, fluorozirconate, fluorotitanate, phospho-tungstate, tungstate, molybdate, and the like, including mixtures and combinations thereof. In addition, other ionic or non-ionic compounds that serve as sources for these electron-withdrawing anions also can be employed in the present invention. It is contemplated that the electron-withdrawing anion can be, or can comprise, fluoride, chloride, bromide, phosphate, triflate, bisulfate, or sulfate, and the like, or any combination thereof, in some aspects of this invention. In other aspects, the electron-withdrawing anion can comprise sulfate, bisulfate, fluoride, chloride, bromide, iodide, fluorosulfate, fluoroborate, phosphate, fluorophosphate, trifluoroacetate, triflate, fluorozirconate, fluorotitanate, tungstate, molybdate, and the like, or combinations thereof.

Thus, for example, the activator-support (or chemically-treated solid oxide) used in the catalyst compositions of the present invention can comprise fluorided alumina, chlorided alumina, bromided alumina, sulfated alumina, fluorided silica-alumina, chlorided silica-alumina, bromided silica-alumina, sulfated silica-alumina, fluorided silica-zirconia, chlorided silica-zirconia, bromided silica-zirconia, sulfated silica-zirconia, fluorided silica-titania, fluorided silica-coated alumina, sulfated silica-coated alumina, phosphated silica-coated alumina, chlorided zinc-coated alumina, molybdate-treated alumina, and the like, or combinations thereof. In one aspect, the activator-support can comprise fluorided alumina, sulfated alumina, fluorided silica-alumina, sulfated silica-alumina, fluorided silica-coated alumina, sulfated silica-coated alumina, phosphated silica-coated alumina, and the like, or any combination thereof. In another aspect, the activator-support can comprise fluorided alumina; alternatively, chlorided alumina; alternatively, sulfated alumina; alternatively, fluorided silica-alumina; alternatively, sulfated silica-alumina; alternatively, fluorided silica-zirconia; alternatively, chlorided silica-zirconia; or alternatively, fluorided silica-coated alumina.

When the electron-withdrawing component comprises a salt of an electron-withdrawing anion, the counterion or cation of that salt can be selected from any cation that allows the salt to revert or decompose back to the acid during calcining. Factors that dictate the suitability of the particular salt to serve as a source for the electron-withdrawing anion can include, but are not limited to, the solubility of the salt in the desired solvent, the lack of adverse reactivity of the cation, ion-pairing effects between the cation and anion, hygroscopic properties imparted to the salt by the cation, and the like, and thermal stability of the anion. Examples of suitable cations in the salt of the electron-withdrawing anion can include, but are not limited to, ammonium, trialkyl ammonium, tetraalkyl ammonium, tetraalkyl phosphonium, H⁺, [H(OEt₂)₂]⁺, and the like.

Further, combinations of one or more different electron-withdrawing anions, in varying proportions, can be used to tailor the specific acidity of the activator-support to the desired level. Combinations of electron-withdrawing components can be contacted with the oxide material simultaneously or individually, and in any order that affords the desired chemically-treated solid oxide acidity. For example, one aspect of this invention can employ two or more electron-withdrawing anion source compounds in two or more separate contacting steps.

Thus, a process by which a chemically-treated solid oxide can be prepared is as follows: a selected solid oxide, or combination of solid oxides, can be contacted with a first electron-withdrawing anion source compound to form a first mixture; this first mixture can be calcined and then contacted with a second electron-withdrawing anion source compound to form a second mixture; the second mixture then can be calcined to form a treated solid oxide. In such a process, the first and second electron-withdrawing anion source compounds can be either the same or different compounds.

According to another aspect of the present invention, the chemically-treated solid oxide can comprise a solid inorganic oxide material, a mixed oxide material, or a combination of inorganic oxide materials, that is chemically-treated with an electron-withdrawing component, and optionally treated with a metal source, including metal salts, metal ions, or other metal-containing compounds. Non-limiting examples of the metal or metal ion can include zinc, nickel, vanadium, titanium, silver, copper, gallium, tin, tungsten, molybdenum, zirconium, boron, and the like, or combinations thereof. Examples of chemically-treated solid oxides that contain a metal or metal ion can include, but are not limited to, chlorided zinc-impregnated alumina, fluorided titanium-impregnated silica, fluorided zinc-impregnated alumina, chlorided zinc-impregnated silica-alumina, fluorided zinc-impregnated silica-alumina, sulfated zinc-impregnated alumina, chlorided zinc aluminate, fluorided zinc aluminate, sulfated zinc aluminate, silica-coated alumina treated with hexafluorotitanic acid, silica-coated alumina treated with zinc and then fluorided, and the like, or any combination thereof. Any method of impregnating the solid oxide material with a metal can be used.

The method by which the oxide is contacted with a metal source, typically a salt or metal-containing compound, can include, but is not limited to, gelling, co-gelling, impregnation of one compound onto another, and the like. If desired, the metal-containing compound can be added to or impregnated into the solid oxide in solution form, and subsequently converted into the supported metal upon calcining. Accordingly, the solid inorganic oxide can further comprise a metal selected from zinc, titanium, nickel, vanadium, silver, copper, gallium, tin, tungsten, molybdenum, and the like, or combinations of these metals. For example, zinc often can be used to impregnate the solid oxide because it can provide improved catalyst activity at a low cost.

The solid oxide can be treated with metal salts or metal-containing compounds before, after, or at the same time that the solid oxide is treated with the electron-withdrawing anion. Following any contacting method, the contacted mixture of solid compound, electron-withdrawing anion, and the metal ion can be calcined. Alternatively, a solid oxide material, an electron-withdrawing anion source, and the metal salt or metal-containing compound can be contacted and calcined simultaneously.

Various processes can be used to form the chemically-treated solid oxide useful in the present invention. The chemically-treated solid oxide can comprise the contact product of one or more solid oxides with one or more electron-withdrawing anion sources. It is not required that the solid oxide be calcined prior to contacting the electron-withdrawing anion source. Typically, the contact product can be calcined either during or after the solid oxide is contacted with the electron-withdrawing anion source. The solid oxide can be calcined or uncalcined. Various processes to prepare solid oxide activator-supports that can be employed in this invention have been reported. For example, such methods are described in U.S. Pat. Nos. 6,107,230, 6,165,929, 6,294,494, 6,300,271, 6,316,553, 6,355,594, 6,376,415, 6,388,017, 6,391,816, 6,395,666, 6,524,987, 6,548,441, 6,548,442, 6,576,583, 6,613,712, 6,632,894, 6,667,274, and 6,750,302, the disclosures of which are incorporated herein by reference in their entirety.

According to one aspect of the present invention, the solid oxide material can be chemically-treated by contacting it with an electron-withdrawing component, typically an electron-withdrawing anion source. Further, the solid oxide material optionally can be chemically treated with a metal ion, and then calcined to form a metal-containing or metal-impregnated chemically-treated solid oxide. According to another aspect of the present invention, the solid oxide material and electron-withdrawing anion source can be contacted and calcined simultaneously.

The method by which the oxide is contacted with the electron-withdrawing component, typically a salt or an acid of an electron-withdrawing anion, can include, but is not limited to, gelling, co-gelling, impregnation of one compound onto another, and the like. Thus, following any contacting method, the contacted mixture of the solid oxide, electron-withdrawing anion, and optional metal ion, can be calcined.

The solid oxide activator-support (i.e., chemically-treated solid oxide) thus can be produced by a process comprising:

1) contacting a solid oxide (or solid oxides) with an electron-withdrawing anion source compound (or compounds) to form a first mixture; and

2) calcining the first mixture to form the solid oxide activator-support.

According to another aspect of the present invention, the solid oxide activator-support (chemically-treated solid oxide) can be produced by a process comprising:

1) contacting a solid oxide (or solid oxides) with a first electron-withdrawing anion source compound to form a first mixture;

2) calcining the first mixture to produce a calcined first mixture;

3) contacting the calcined first mixture with a second electron-withdrawing anion source compound to form a second mixture; and

4) calcining the second mixture to form the solid oxide activator-support.

According to yet another aspect of the present invention, the chemically-treated solid oxide can be produced or formed by contacting the solid oxide with the electron-withdrawing anion source compound, where the solid oxide compound is calcined before, during, or after contacting the electron-withdrawing anion source, and where there is a substantial absence of aluminoxanes, organoboron or organoborate compounds, and ionizing ionic compounds.

Calcining of the treated solid oxide generally can be conducted in an ambient atmosphere, typically in a dry ambient atmosphere, at a temperature from about 200° C. to about 900° C., and for a time of about 1 minute to about 100 hours. Calcining can be conducted at a temperature of from about 300° C. to about 800° C., or alternatively, at a temperature of from about 400° C. to about 700° C. Calcining can be conducted for about 30 minutes to about 50 hours, or for about 1 hour to about 15 hours. Thus, for example, calcining can be carried out for about 1 to about 10 hours at a temperature of from about 350° C. to about 550° C. Any suitable ambient atmosphere can be employed during calcining. Generally, calcining can be conducted in an oxidizing atmosphere, such as air. Alternatively, an inert atmosphere, such as nitrogen or argon, or a reducing atmosphere, such as hydrogen or carbon monoxide, can be used.

According to one aspect of the present invention, the solid oxide material can be treated with a source of halide ion, sulfate ion, or a combination of anions, optionally treated with a metal ion, and then calcined to provide the chemically-treated solid oxide in the form of a particulate solid. For example, the solid oxide material can be treated with a source of sulfate (termed a “sulfating agent”), a source of bromide ion (termed a “bromiding agent”), a source of chloride ion (termed a “chloriding agent”), a source of fluoride ion (termed a “fluoriding agent”), or a combination thereof, and calcined to provide the solid oxide activator. Useful acidic activator-supports can include, but are not limited to, bromided alumina, chlorided alumina, fluorided alumina, sulfated alumina, bromided silica-alumina, chlorided silica-alumina, fluorided silica-alumina, sulfated silica-alumina, bromided silica-zirconia, chlorided silica-zirconia, fluorided silica-zirconia, sulfated silica-zirconia, fluorided silica-titania, alumina treated with hexafluorotitanic acid, silica-coated alumina treated with hexafluorotitanic acid, silica-alumina treated with hexafluorozirconic acid, silica-alumina treated with trifluoroacetic acid, fluorided boria-alumina, silica treated with tetrafluoroboric acid, alumina treated with tetrafluoroboric acid, alumina treated with hexafluorophosphoric acid, a pillared clay, such as a pillared montmorillonite, optionally treated with fluoride, chloride, or sulfate; phosphated alumina or other aluminophosphates optionally treated with sulfate, fluoride, or chloride; or any combination of the above. Further, any of these activator-supports optionally can be treated or impregnated with a metal ion.

In an aspect, the chemically-treated solid oxide can comprise a fluorided solid oxide in the form of a particulate solid. The fluorided solid oxide can be formed by contacting a solid oxide with a fluoriding agent. The fluoride ion can be added to the oxide by forming a slurry of the oxide in a suitable solvent such as alcohol or water including, but not limited to, the one to three carbon alcohols because of their volatility and low surface tension. Examples of suitable fluoriding agents can include, but are not limited to, hydrofluoric acid (HF), ammonium fluoride (NH₄F), ammonium bifluoride (NH₄HF₂), ammonium tetrafluoroborate (NH₄BF₄), ammonium silicofluoride (hexafluorosilicate) ((NH₄)₂SiF₆), ammonium hexafluorophosphate (NH₄PF₆), hexafluorotitanic acid (H₂TiF₆), ammonium hexafluorotitanic acid ((NH₄)₂TiF₆), hexafluorozirconic acid (H₂ZrF₆), AlF₃, NH₄AlF₄, analogs thereof, and combinations thereof. Triflic acid and ammonium triflate also can be employed. For example, ammonium bifluoride (NH₄HF₂) can be used as the fluoriding agent, due to its ease of use and availability. In some aspects, the solid oxide can be dry-mixed with a fluoride salt, which then decomposes and vaporizes during calcination.

If desired, the solid oxide can be treated with a fluoriding agent during the calcining step. Any fluoriding agent capable of thoroughly contacting the solid oxide during the calcining step can be used. For example, in addition to those fluoriding agents described previously, volatile organic fluoriding agents can be used. Examples of volatile organic fluoriding agents useful in this aspect of the invention can include, but are not limited to, freons, perfluorohexane, perfluorobenzene, fluoromethane, trifluoroethanol, and the like, and combinations thereof. Calcining temperatures generally must be high enough to decompose the compound and release fluoride. Gaseous hydrogen fluoride (HF) or fluorine (F₂) itself also can be used with the solid oxide if fluorided while calcining. Silicon tetrafluoride (SiF₄) and compounds containing tetrafluoroborate (BF₄ ⁻) also can be employed. One convenient method of contacting the solid oxide with the fluoriding agent can be to vaporize a fluoriding agent into a gas stream used to fluidize the solid oxide during calcination.

Similarly, in another aspect of this invention, the chemically-treated solid oxide can comprise a chlorided solid oxide in the form of a particulate solid. The chlorided solid oxide can be formed by contacting a solid oxide with a chloriding agent. The chloride ion can be added to the oxide by forming a slurry of the oxide in a suitable solvent. The solid oxide can be treated with a chloriding agent during the calcining step. Any chloriding agent capable of serving as a source of chloride and thoroughly contacting the oxide during the calcining step can be used, such as SiCl₄, SiMe₂Cl₂, TiCl₄, BCl₃, and the like, including mixtures thereof. Volatile organic chloriding agents can be used. Examples of suitable volatile organic chloriding agents can include, but are not limited to, certain freons, perchlorobenzene, chloromethane, dichloromethane, dichloroethane, chloroform, carbon tetrachloride, trichloroethanol, and the like, or any combination thereof. Gaseous hydrogen chloride or chlorine (Cl₂) itself also can be used with the solid oxide during calcining. One convenient method of contacting the oxide with the chloriding agent can be to vaporize a chloriding agent into a gas stream used to fluidize the solid oxide during calcination.

The amount of fluoride or chloride ion present before calcining the solid oxide generally can be from about 1 to about 50% by weight, where the weight percent is based on the weight of the solid oxide, for example, silica-alumina, before calcining. According to another aspect of this invention, the amount of fluoride or chloride ion present before calcining the solid oxide can be from about 1 to about 25% by weight, and according to another aspect of this invention, from about 2 to about 20% by weight. According to yet another aspect of this invention, the amount of fluoride or chloride ion present before calcining the solid oxide can be from about 5 to about 15% by weight. Once impregnated with halide, the halided oxide can be dried by any suitable method including, but not limited to, suction filtration followed by evaporation, drying under vacuum, spray drying, and the like, although it is also possible to initiate the calcining step immediately without drying the impregnated solid oxide.

The silica-alumina used to prepare the treated silica-alumina typically can have a pore volume greater than about 0.5 cc/g. According to one aspect of the present invention, the pore volume can be greater than about 0.8 cc/g, and according to another aspect of the present invention, greater than about 1.0 cc/g. Further, the silica-alumina generally can have a surface area greater than about 100 m²/g. According to another aspect of this invention, the surface area can be greater than about 250 m²/g. Yet, in another aspect, the surface area can be greater than about 350 m²/g.

The silica-alumina utilized in the present invention typically can have an alumina content from about 5 to about 95% by weight. According to one aspect of this invention, the alumina content of the silica-alumina can be from about 5 to about 50%, or from about 8% to about 30%, alumina by weight. In another aspect, high alumina content silica-alumina compounds can be employed, in which the alumina content of these silica-alumina compounds typically ranges from about 60% to about 90%, or from about 65% to about 80%, alumina by weight. According to yet another aspect of this invention, the solid oxide component can comprise alumina without silica, and according to another aspect of this invention, the solid oxide component can comprise silica without alumina.

The sulfated solid oxide can comprise sulfate and a solid oxide component, such as alumina or silica-alumina, in the form of a particulate solid. Optionally, the sulfated oxide can be treated further with a metal ion such that the calcined sulfated oxide comprises a metal. According to one aspect of the present invention, the sulfated solid oxide can comprise sulfate and alumina. In some instances, the sulfated alumina can be formed by a process wherein the alumina is treated with a sulfate source, for example, sulfuric acid or a sulfate salt such as ammonium sulfate. This process generally can be performed by forming a slurry of the alumina in a suitable solvent, such as alcohol or water, in which the desired concentration of the sulfating agent has been added. Suitable organic solvents can include, but are not limited to, the one to three carbon alcohols because of their volatility and low surface tension.

According to one aspect of this invention, the amount of sulfate ion present before calcining can be from about 0.5 to about 100 parts by weight sulfate ion to about 100 parts by weight solid oxide. According to another aspect of this invention, the amount of sulfate ion present before calcining can be from about 1 to about 50 parts by weight sulfate ion to about 100 parts by weight solid oxide, and according to still another aspect of this invention, from about 5 to about 30 parts by weight sulfate ion to about 100 parts by weight solid oxide. These weight ratios are based on the weight of the solid oxide before calcining. Once impregnated with sulfate, the sulfated oxide can be dried by any suitable method including, but not limited to, suction filtration followed by evaporation, drying under vacuum, spray drying, and the like, although it is also possible to initiate the calcining step immediately.

The activator-support used to prepare the catalyst compositions of the present invention can be combined with other inorganic support materials, including, but not limited to, zeolites, inorganic oxides, and the like. In one aspect, typical support materials that can be used include, but are not limited to, silica, silica-alumina, alumina, titania, zirconia, magnesia, boria, thoria, aluminophosphate, aluminum phosphate, silica-titania, coprecipitated silica/titania, mixtures thereof, or any combination thereof.

According to another aspect of the present invention, a metallocene compound can be precontacted with an olefin monomer and an organoaluminum compound for a first period of time prior to contacting this mixture with the activator-supports. Once the precontacted mixture of metallocene complex, olefin monomer, and organoaluminum compound is contacted with the activator-supports, the composition further comprising the activator-supports can be termed a “postcontacted” mixture. The postcontacted mixture can be allowed to remain in further contact for a second period of time prior to being charged into the reactor in which the polymerization process will be carried out.

According to yet another aspect of the present invention, a metallocene compound can be precontacted with an olefin monomer and one or more of the activator-support(s) for a first period of time prior to contacting this mixture with the organoaluminum compound. Once the precontacted mixture of the metallocene complex, olefin monomer, and activator-support(s) is contacted with the organoaluminum compound, the composition further comprising the organoaluminum can be termed a “postcontacted” mixture. The postcontacted mixture can be allowed to remain in further contact for a second period of time prior to being introduced into the polymerization reactor.

Activator-Support I and Activator-Support II

In accordance with aspects of the present invention, catalyst compositions can comprise activator-support I and activator-support II. Activator-support I can comprise a halided solid oxide, while activator-support II can comprise a sulfated solid oxide, a phosphated solid oxide, or a combination thereof. Hence, activator-support I can comprise a fluorided solid oxide, a chlorided solid oxide, a bromided solid oxide, an iodided solid oxide, or any combination thereof; alternatively, a fluorided solid oxide; alternatively, a chlorided solid oxide; alternatively, a bromided solid oxide; or alternatively, an iodided solid oxide. Likewise, activator-support II can comprise a sulfated solid oxide, a phosphated solid oxide, or a combination thereof; alternatively, a sulfated solid oxide; or alternatively, a phosphated solid oxide.

As discussed herein, the solid oxide of the halided solid oxide, the sulfated solid oxide, and the phosphated solid oxide independently can comprise silica, alumina, silica-alumina, silica-coated alumina, aluminum phosphate, aluminophosphate, heteropolytungstate, titania, zirconia, magnesia, boria, zinc oxide, and the like, as well as any mixed oxide thereof, or any mixture thereof. In an aspect, the solid oxide of the halided solid oxide, the sulfated solid oxide, and the phosphated solid oxide independently can comprise alumina, silica-alumina, silica-coated alumina, or a mixture thereof; alternatively, alumina; alternatively, silica-alumina; or alternatively, silica-coated alumina.

In one aspect, activator-support I can comprise fluorided alumina, and activator-support II can comprise sulfated alumina. In another aspect, activator-support I can comprise fluorided alumina, and activator-support II can comprise phosphated alumina. In another aspect, activator-support I can comprise chlorided alumina, and activator-support II can comprise sulfated alumina. In another aspect, activator-support I can comprise chlorided alumina, and activator-support II can comprise phosphated alumina. In another aspect, activator-support I can comprise fluorided silica-alumina, and activator-support II can comprise sulfated silica-alumina. In another aspect, activator-support I can comprise fluorided silica-alumina, and activator-support II can comprise phosphated silica-alumina. In another aspect, activator-support I can comprise chlorided silica-alumina, and activator-support II can comprise sulfated silica-alumina. In another aspect, activator-support I can comprise chlorided silica-alumina, and activator-support II can comprise phosphated silica-alumina. In another aspect, activator-support I can comprise fluorided silica-coated alumina, and activator-support II can comprise sulfated silica-coated alumina. In another aspect, activator-support I can comprise fluorided silica-coated alumina, and activator-support II can comprise phosphated silica-coated alumina. In another aspect, activator-support I can comprise chlorided silica-coated alumina, and activator-support II can comprise sulfated silica-coated alumina. In another aspect, activator-support I can comprise chlorided silica-coated alumina, and activator-support II can comprise phosphated silica-coated alumina. In yet another aspect, activator-support I can comprise fluorided silica-alumina, and activator-support II can comprise sulfated alumina, while in still another aspect, activator-support I can comprise fluorided silica-coated alumina, and activator-support II can comprise sulfated alumina.

The weight ratio of activator-support I to activator-support II in the catalyst system generally is not limited to any particular range of weight ratios. Nonetheless, in some aspects, the weight ratio of activator-support I to activator-support II can be in a range of from about 1:100 to about 100:1, from about 1:50 to about 50:1, from about 1:25 to about 25:1, from about 1:10 to about 10:1, or from about 1:5 to about 5:1. Accordingly, suitable ranges for the weight ratio of activator-support I to activator-support II can include, but are not limited to, from about 1:15 to about 15:1, from about 1:10 to about 10:1, from about 1:8 to about 8:1, from about 1:5 to about 5:1, from about 1:4 to about 4:1, from about 1:3 to about 3:1, from about 1:2 to about 2:1, from about 1:1.8 to about 1.8:1, from about 1:1.5 to about 1.5:1, from about 1:1.3 to about 1.3:1, from about 1:1.25 to about 1.25:1, from about 1:1.2 to about 1.2:1, from about 1:1.15 to about 1.15:1, from about 1:1.1 to about 1.1:1, or from about 1:1.05 to about 1.05:1, and the like.

Co-Catalysts

In certain aspects directed to catalyst compositions containing a co-catalyst, the co-catalyst can comprise a metal hydrocarbyl compound, examples of which include non-halide metal hydrocarbyl compounds, metal hydrocarbyl halide compounds, non-halide metal alkyl compounds, metal alkyl halide compounds, and so forth. The hydrocarbyl group (or alkyl group) can be any hydrocarbyl (or alkyl) group disclosed herein. Moreover, in some aspects, the metal of the metal hydrocarbyl can be a group 1, 2, 11, 12, 13, or 14 metal; alternatively, a group 13 or 14 metal; or alternatively, a group 13 metal. Hence, in some aspects, the metal of the metal hydrocarbyl (non-halide metal hydrocarbyl or metal hydrocarbyl halide) can be lithium, sodium, potassium, rubidium, cesium, beryllium, magnesium, calcium, strontium, barium, zinc, cadmium, boron, aluminum, or tin; alternatively, lithium, sodium, potassium, magnesium, calcium, zinc, boron, aluminum, or tin; alternatively, lithium, sodium, or potassium; alternatively, magnesium or calcium; alternatively, lithium; alternatively, sodium; alternatively, potassium; alternatively, magnesium; alternatively, calcium; alternatively, zinc; alternatively, boron; alternatively, aluminum; or alternatively, tin. In some aspects, the metal hydrocarbyl or metal alkyl, with or without a halide, can comprise a lithium hydrocarbyl or alkyl, a magnesium hydrocarbyl or alkyl, a boron hydrocarbyl or alkyl, a zinc hydrocarbyl or alkyl, or an aluminum hydrocarbyl or alkyl.

In particular aspects directed to catalyst compositions containing activator-support I and activator-support II, the co-catalyst can comprise an aluminoxane compound, an organoboron or organoborate compound, an ionizing ionic compound, an organoaluminum compound, an organozinc compound, an organomagnesium compound, or an organolithium compound, and this includes any combinations of these materials. In one aspect, the co-catalyst can comprise an organoaluminum compound. In another aspect, the co-catalyst can comprise an aluminoxane compound, an organoboron or organoborate compound, an ionizing ionic compound, an organozinc compound, an organomagnesium compound, an organolithium compound, or any combination thereof. In yet another aspect, the co-catalyst can comprise an aluminoxane compound; alternatively, an organoboron or organoborate compound; alternatively, an ionizing ionic compound; alternatively, an organozinc compound; alternatively, an organomagnesium compound; or alternatively, an organolithium compound.

Organoaluminum Compounds

In some aspects, catalyst compositions of the present invention can comprise one or more organoaluminum compounds. Such compounds can include, but are not limited to, compounds having the formula: (R^(Z))₃Al; where each R^(Z) independently can be an aliphatic group having from 1 to 10 carbon atoms. For example, each R^(Z) independently can be methyl, ethyl, propyl, butyl, hexyl, or isobutyl.

Other organoaluminum compounds which can be used in catalyst compositions disclosed herein can include, but are not limited to, compounds having the formula: Al(X⁷)_(m)(X⁸)_(3-m), where each X⁷ independently can be a hydrocarbyl; each X⁸ independently can be an alkoxide or an aryloxide, a halide, or a hydride; and m can be from 1 to 3, inclusive. Hydrocarbyl is used herein to specify a hydrocarbon radical group and includes, for instance, aryl, alkyl, cycloalkyl, alkenyl, cycloalkenyl, cycloalkadienyl, alkynyl, aralkyl, aralkenyl, and aralkynyl groups.

In one aspect, each X⁷ independently can be any hydrocarbyl having from 1 to about 18 carbon atoms disclosed herein. In another aspect of the present invention, each X⁷ independently can be any alkyl having from 1 to 10 carbon atoms disclosed herein. For example, each X⁷ independently can be methyl, ethyl, propyl, n-butyl, sec-butyl, isobutyl, or hexyl, and the like, in yet another aspect of the present invention.

According to one aspect of the present invention, each X⁸ independently can be an alkoxide or an aryloxide, any one of which has from 1 to 18 carbon atoms, a halide, or a hydride. In another aspect of the present invention, each X⁸ can be selected independently from fluorine and chlorine. Yet, in another aspect, X⁸ can be chlorine.

In the formula, Al(X⁷)_(m)(X⁸)_(3-m), m can be a number from 1 to 3, inclusive, and typically, m can be 3. The value of m is not restricted to be an integer; therefore, this formula can include sesquihalide compounds or other organoaluminum cluster compounds.

Examples of organoaluminum compounds suitable for use in accordance with the present invention can include, but are not limited to, trialkylaluminum compounds, dialkylaluminum halide compounds, dialkylaluminum alkoxide compounds, dialkylaluminum hydride compounds, and combinations thereof. Specific non-limiting examples of suitable organoaluminum compounds can include trimethylaluminum (TMA), triethylaluminum (TEA), tri-n-propylaluminum (TNPA), tri-n-butylaluminum (TNBA), triisobutylaluminum (TIBA), tri-n-hexylaluminum, tri-n-octylaluminum, diisobutylaluminum hydride, diethylaluminum ethoxide, diethylaluminum chloride, and the like, or combinations thereof.

The present invention contemplates a method of precontacting a metallocene compound (or compounds) with an organoaluminum compound and an olefin monomer to form a precontacted mixture, prior to contacting this precontacted mixture with the activator-supports to form a catalyst composition. When the catalyst composition is prepared in this manner, typically, though not necessarily, a portion of the organoaluminum compound can be added to the precontacted mixture and another portion of the organoaluminum compound can be added to the postcontacted mixture prepared when the precontacted mixture is contacted with the solid oxide activator-supports. However, the entire organoaluminum compound can be used to prepare the catalyst composition in either the precontacting or postcontacting step. Alternatively, all the catalyst components can be contacted in a single step.

Further, more than one organoaluminum compound can be used in either the precontacting or the postcontacting step. When an organoaluminum compound is added in multiple steps, the amounts of organoaluminum compound disclosed herein include the total amount of organoaluminum compound used in both the precontacted and postcontacted mixtures, and any additional organoaluminum compound added to the polymerization reactor. Therefore, total amounts of organoaluminum compounds are disclosed regardless of whether a single organoaluminum compound or more than one organoaluminum compound is used.

Aluminoxane Compounds

Certain aspects of the present invention provide a catalyst composition which can comprise an aluminoxane compound. As used herein, the terms “aluminoxane” and “aluminoxane compound” refer to aluminoxane compounds, compositions, mixtures, or discrete species, regardless of how such aluminoxanes are prepared, formed or otherwise provided. For example, a catalyst composition comprising an aluminoxane compound can be prepared in which aluminoxane is provided as the poly(hydrocarbyl aluminum oxide), or in which aluminoxane is provided as the combination of an aluminum alkyl compound and a source of active protons such as water. Aluminoxanes also can be referred to as poly(hydrocarbyl aluminum oxides) or organoaluminoxanes.

The other catalyst components typically can be contacted with the aluminoxane in a saturated hydrocarbon compound solvent, though any solvent that is substantially inert to the reactants, intermediates, and products of the activation step can be used. The catalyst composition formed in this manner can be collected by any suitable method, for example, by filtration. Alternatively, the catalyst composition can be introduced into the polymerization reactor without being isolated.

The aluminoxane compound of this invention can be an oligomeric aluminum compound comprising linear structures, cyclic structures, or cage structures, or mixtures of all three. Cyclic aluminoxane compounds having the formula:

wherein each R in this formula independently can be a linear or branched alkyl having from 1 to 10 carbon atoms, and p in this formula can be an integer from 3 to 20, are encompassed by this invention. The AlRO moiety shown here also can constitute the repeating unit in a linear aluminoxane. Thus, linear aluminoxanes having the formula:

wherein each R in this formula independently can be a linear or branched alkyl having from 1 to 10 carbon atoms, and q in this formula can be an integer from 1 to 50, are also encompassed by this invention.

Further, aluminoxanes can have cage structures of the formula R^(t) _(5r+α)R^(b) _(r−α)Al_(4r)O_(3r), wherein each R^(t) independently can be a terminal linear or branched alkyl group having from 1 to 10 carbon atoms; each R^(b) independently can be a bridging linear or branched alkyl group having from 1 to 10 carbon atoms; r can be 3 or 4; and a can be equal to n_(Al(3))−n_(O(2))+n_(O(4)), wherein n_(Al(3)) is the number of three coordinate aluminum atoms, n_(O(2)) is the number of two coordinate oxygen atoms, and n_(O(4)) is the number of 4 coordinate oxygen atoms.

Thus, aluminoxanes which can be employed in the catalyst compositions of the present invention can be represented generally by formulas such as (R—Al—O)_(p), R(R—Al—O)_(q)AlR₂, and the like. In these formulas, each R group independently can be a linear or branched C₁-C₆ alkyl, such as methyl, ethyl, propyl, butyl, pentyl, or hexyl. Examples of aluminoxane compounds that can be used in accordance with the present invention can include, but are not limited to, methylaluminoxane, modified methylaluminoxane, ethylaluminoxane, n-propylaluminoxane, iso-propylaluminoxane, n-butylaluminoxane, t-butylaluminoxane, sec-butylaluminoxane, iso-butylaluminoxane, 1-pentylaluminoxane, 2-pentylaluminoxane, 3-pentylaluminoxane, isopentylaluminoxane, neopentylaluminoxane, and the like, or any combination thereof. Methylaluminoxane, ethylaluminoxane, and iso-butylaluminoxane can be prepared from trimethylaluminum, triethylaluminum, or triisobutylaluminum, respectively, and sometimes are referred to as poly(methyl aluminum oxide), poly(ethyl aluminum oxide), and poly(isobutyl aluminum oxide), respectively. It is also within the scope of the invention to use an aluminoxane in combination with a trialkylaluminum, such as that disclosed in U.S. Pat. No. 4,794,096, incorporated herein by reference in its entirety.

The present invention contemplates many values of p and q in the aluminoxane formulas (R—Al—O)_(p) and R(R—Al—O)_(q)AlR₂, respectively. In some aspects, p and q can be at least 3. However, depending upon how the organoaluminoxane is prepared, stored, and used, the value of p and q can vary within a single sample of aluminoxane, and such combinations of organoaluminoxanes are contemplated herein.

In preparing a catalyst composition containing an aluminoxane, the molar ratio of the total moles of aluminum in the aluminoxane (or aluminoxanes) to the total moles of metallocene complex(es) in the composition generally can be between about 1:10 and about 100,000:1. In another aspect, the molar ratio can be in a range from about 5:1 to about 15,000:1. Optionally, aluminoxane can be added to a polymerization reactor system in ranges from about 0.01 mg/L to about 1000 mg/L, from about 0.1 mg/L to about 100 mg/L, or from about 1 mg/L to about 50 mg/L.

Organoaluminoxanes can be prepared by various procedures. Examples of organoaluminoxane preparations are disclosed in U.S. Pat. Nos. 3,242,099 and 4,808,561, the disclosures of which are incorporated herein by reference in their entirety. For example, water in an inert organic solvent can be reacted with an aluminum alkyl compound, such as (R^(Z))₃Al, to form the desired organoaluminoxane compound. While not intending to be bound by this statement, it is believed that this synthetic method can afford a mixture of both linear and cyclic R—Al—O aluminoxane species, both of which are encompassed by this invention. Alternatively, organoaluminoxanes can be prepared by reacting an aluminum alkyl compound, such as (R^(Z))₃Al, with a hydrated salt, such as hydrated copper sulfate, in an inert organic solvent.

Organoboron & Organoborate Compounds

According to another aspect of the present invention, the catalyst composition can comprise an organoboron or organoborate compound. Such compounds can include neutral boron compounds, borate salts, and the like, or combinations thereof. For example, fluoroorgano boron compounds and fluoroorgano borate compounds are contemplated.

Any fluoroorgano boron or fluoroorgano borate compound can be utilized with the present invention. Examples of fluoroorgano borate compounds that can be used in the present invention can include, but are not limited to, fluorinated aryl borates such as N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate, triphenylcarbenium tetrakis(pentafluorophenyl)borate, lithium tetrakis(pentafluorophenyl)borate, N,N-dimethylanilinium tetrakis[3,5-bis(trifluoromethyl)phenyl]borate, triphenylcarbenium tetrakis[3,5-bis(trifluoromethyl)phenyl]borate, and the like, or mixtures thereof. Examples of fluoroorgano boron compounds that can be used as co-catalysts in the present invention can include, but are not limited to, tris(pentafluorophenyl)boron, tris[3,5-bis(trifluoromethyl)phenyl]boron, and the like, or mixtures thereof. Although not intending to be bound by the following theory, these examples of fluoroorgano borate and fluoroorgano boron compounds, and related compounds, can form “weakly-coordinating” anions when combined with a transition metal complex (see e.g., U.S. Pat. No. 5,919,983, the disclosure of which is incorporated herein by reference in its entirety). Applicants also contemplate the use of diboron, or bis-boron, compounds or other bifunctional compounds containing two or more boron atoms in the chemical structure, such as disclosed in J. Am. Chem. Soc., 2005, 127, pp. 14756-14768, the content of which is incorporated herein by reference in its entirety.

Generally, any amount of organoboron compound can be used. According to one aspect of this invention, the molar ratio of the total moles of organoboron or organoborate compound (or compounds) to the total moles of metallocene compound(s) in the catalyst composition can be in a range from about 0.1:1 to about 15:1. Typically, the amount of the fluoroorgano boron or fluoroorgano borate compound used can be from about 0.5 moles to about 10 moles of boron/borate compound per mole of metallocene complex(es). According to another aspect of this invention, the amount of fluoroorgano boron or fluoroorgano borate compound can be from about 0.8 moles to about 5 moles of boron/borate compound per mole of metallocene complex(es).

Ionizing Ionic Compounds

In another aspect, catalyst compositions disclosed herein can comprise an ionizing ionic compound. An ionizing ionic compound is an ionic compound that can function as a co-catalyst to enhance the activity of the catalyst composition. While not intending to be bound by theory, it is believed that the ionizing ionic compound can be capable of reacting with a metallocene complex and converting the metallocene complex into one or more cationic metallocene complexes, or incipient cationic metallocene complexes. Again, while not intending to be bound by theory, it is believed that the ionizing ionic compound can function as an ionizing compound by completely or partially extracting an anionic ligand, such as a monoanionic ligand (e.g. chlorine, etc.), from the metallocene complex. However, the ionizing ionic compound can be a co-catalyst regardless of whether it is ionizes the metallocene compound, abstracts a ligand in a fashion as to form an ion pair, weakens the metal-ligand bond in the metallocene, simply coordinates to a ligand, or activates the metallocene by some other mechanism.

Further, it is not necessary that the ionizing ionic compound activate the metallocene compound only. The activation function of the ionizing ionic compound can be evident in the enhanced activity of catalyst composition as a whole, as compared to a catalyst composition that does not contain an ionizing ionic compound. Examples of ionizing ionic compounds can include, but are not limited to, the following compounds: tri(n-butyl)ammonium tetrakis(p-tolyl)borate, tri(n-butyl)ammonium tetrakis(m-tolyl)borate, tri(n-butyl)ammonium tetrakis(2,4-dimethylphenyl)borate, tri(n-butyl)ammonium tetrakis(3,5-dimethylphenyl)_(b) orate, tri(n-butyl)ammonium tetrakis[3,5-bis(trifluoromethyl)phenyl]borate, tri(n-butyl)ammonium tetrakis(pentafluorophenyl)borate, N,N-dimethylanilinium tetrakis(p-tolyl)borate, N,N-dimethylanilinium tetrakis(m-tolyl)borate, N,N-dimethylanilinium tetrakis(2,4-dimethylphenyl)borate, N,N-dimethylanilinium tetrakis(3,5-dimethyl-phenyl)borate, N,N-dimethylanilinium tetrakis[3,5-bis(trifluoromethyl)phenyl]borate, N,N-dimethylanilinium tetrakis(pentafluorophenyl)borate, triphenylcarbenium tetrakis(p-tolyl)borate, triphenylcarbenium tetrakis(m-tolyl)borate, triphenylcarbenium tetrakis(2,4-dimethylphenyl)borate, triphenylcarbenium tetrakis(3,5-dimethylphenyl)borate, triphenylcarbenium tetrakis[3,5-bis(trifluoromethyl)phenyl]borate, triphenylcarbenium tetrakis(pentafluorophenyl)borate, tropylium tetrakis(p-tolyl)borate, tropylium tetrakis(m-tolyl)borate, tropylium tetrakis(2,4-dimethylphenyl)borate, tropylium tetrakis(3,5-dimethylphenyl)borate, tropylium tetrakis[3,5-bis(trifluoromethyl)phenyl]borate, tropylium tetrakis(pentafluorophenyl)borate, lithium tetrakis(pentafluorophenyl)borate, lithium tetraphenylborate, lithium tetrakis(p-tolyl)borate, lithium tetrakis(m-tolyl)borate, lithium tetrakis(2,4-dimethylphenyl)borate, lithium tetrakis(3,5-dimethylphenyl)borate, lithium tetrafluoroborate, sodium tetrakis(pentafluorophenyl)borate, sodium tetraphenylborate, sodium tetrakis(p-tolyl)borate, sodium tetrakis(m-tolyl)borate, sodium tetrakis(2,4-dimethylphenyl)borate, sodium tetrakis(3,5-dimethylphenyl)borate, sodium tetrafluoroborate, potassium tetrakis(pentafluorophenyl)borate, potassium tetraphenylborate, potassium tetrakis(p-tolyl)borate, potassium tetrakis(m-tolyl)borate, potassium tetrakis(2,4-dimethylphenyl)borate, potassium tetrakis(3,5-dimethylphenyl)borate, potassium tetrafluoroborate, lithium tetrakis(pentafluorophenyl)aluminate, lithium tetraphenylaluminate, lithium tetrakis(p-tolyl)aluminate, lithium tetrakis(m-tolyl)aluminate, lithium tetrakis(2,4-dimethylphenyl)aluminate, lithium tetrakis(3,5-dimethylphenyl)aluminate, lithium tetrafluoroaluminate, sodium tetrakis(pentafluorophenyl)aluminate, sodium tetraphenylaluminate, sodium tetrakis(p-tolyl)aluminate, sodium tetrakis(m-tolyl)aluminate, sodium tetrakis(2,4-dimethylphenyl)aluminate, sodium tetrakis(3,5-dimethylphenyl)aluminate, sodium tetrafluoroaluminate, potassium tetrakis(pentafluorophenyl)aluminate, potassium tetraphenylaluminate, potassium tetrakis(p-tolyl)aluminate, potassium tetrakis(m-tolyl)aluminate, potassium tetrakis(2,4-dimethylphenyl)aluminate, potassium tetrakis (3,5-dimethylphenyl)aluminate, potassium tetrafluoroaluminate, and the like, or combinations thereof. Ionizing ionic compounds useful in this invention are not limited to these; other examples of ionizing ionic compounds are disclosed in U.S. Pat. Nos. 5,576,259 and 5,807,938, the disclosures of which are incorporated herein by reference in their entirety.

Organozinc, Organomagnesium, & Organolithium Compounds

Other aspects are directed to catalyst compositions which can include an organozinc compound, an organomagnesium compound, an organolithium compound, or a combination thereof. In some aspects, these compounds have the following general formulas: Zn(X¹⁰)(X¹¹); Mg(X¹²)(X¹³); and Li(X¹⁴). In these formulas, X¹⁰, X¹², and X¹⁴ independently can be a C₁ to C₁₈ hydrocarbyl group, and X¹¹ and X¹³ independently can be H, a halide, or a C₁ to C₁₈ hydrocarbyl or C₁ to C₁₈ hydrocarboxy group. It is contemplated X¹⁰ and X¹¹ (or X¹² and X¹³) can be the same, or that X¹⁰ and X¹¹ (or X¹² and X¹³) can be different.

In one aspect, X¹⁰, X¹¹, X¹², X¹³, and X¹⁴ independently can be any C₁ to C₁₈ hydrocarbyl group, C₁ to C₁₂ hydrocarbyl group, C₁ to C₈ hydrocarbyl group, or C₁ to C₅ hydrocarbyl group disclosed herein. In another aspect, X¹⁰, X¹¹, X¹², X¹³, and X¹⁴ independently can be any C₁ to C₁₈ alkyl group, C₂ to C₁₈ alkenyl group, C₆ to C₁₈ aryl group, or C₇ to C₁₈ aralkyl group disclosed herein; alternatively, any C₁ to C₁₂ alkyl group, C₂ to C₁₂ alkenyl group, C₆ to C₁₂ aryl group, or C₇ to C₁₂ aralkyl group disclosed herein; or alternatively, any C₁ to C₅ alkyl group, C₂ to C₅ alkenyl group, C₆ to C₈ aryl group, or C₇ to C₈ aralkyl group disclosed herein. Thus, X¹⁰, X¹¹, X¹², X¹³, and X¹⁴ independently can be a methyl group, an ethyl group, a propyl group, a butyl group, a pentyl group, a hexyl group, a heptyl group, an octyl group, a nonyl group, a decyl group, a undecyl group, a dodecyl group, a tridecyl group, a tetradecyl group, a pentadecyl group, a hexadecyl group, a heptadecyl group, an octadecyl group, an ethenyl group, a propenyl group, a butenyl group, a pentenyl group, a hexenyl group, a heptenyl group, an octenyl group, a nonenyl group, a decenyl group, a undecenyl group, a dodecenyl group, a tridecenyl group, a tetradecenyl group, a pentadecenyl group, a hexadecenyl group, a heptadecenyl group, an octadecenyl group, a phenyl group, a naphthyl group, a benzyl group, or a tolyl group, and the like. In yet another aspect, X¹⁰, X¹¹, X¹², X¹³, and X¹⁴ independently can be methyl, ethyl, propyl, butyl, or pentyl (e.g., neopentyl), or both X¹⁰ and X¹¹ (or both X¹² and X¹³) can be methyl, or ethyl, or propyl, or butyl, or pentyl (e.g., neopentyl).

X¹¹ and X¹³ independently can be H, a halide, or a C₁ to C₁₈ hydrocarbyl or C₁ to C₁₈ hydrocarboxy group (e.g., any C₁ to C₁₈, C₁ to C₁₂, C₁ to C₁₀, or C₁ to C₈ hydrocarboxy group disclosed herein). In some aspects, X¹¹ and X¹³ independently can be H, a halide (e.g., Cl), or a C₁ to C₁₈ hydrocarbyl or C₁ to C₁₈ hydrocarboxy group; alternatively, H, a halide, or a C₁ to C₈ hydrocarbyl or C₁ to C₈ hydrocarboxy group; or alternatively, H, Br, Cl, F, I, methyl, ethyl, propyl, butyl, pentyl (e.g., neopentyl), hexyl, heptyl, octyl, nonyl, decyl, ethenyl, propenyl, butenyl, pentenyl, hexenyl, heptenyl, octenyl, nonenyl, decenyl, phenyl, benzyl, tolyl, methoxy, ethoxy, propoxy, butoxy, pentoxy, phenoxy, toloxy, xyloxy, or benzoxy.

In other aspects, the organozinc and/or the organomagnesium compound can have one or two hydrocarbylsilyl moieties. Each hydrocarbyl of the hydrocarbylsilyl group can be any hydrocarbyl group disclosed herein (e.g., a C₁ to C₁₈ alkyl group, a C₂ to C₁₈ alkenyl group, a C₆ to C₁₈ aryl group, a C₇ to C₁₈ aralkyl group, etc.). Illustrative and non-limiting examples of hydrocarbylsilyl groups can include, but are not limited to, trimethylsilyl, triethylsilyl, tripropylsilyl (e.g., triisopropylsilyl), tributylsilyl, tripentylsilyl, triphenylsilyl, allyldimethylsilyl, trimethylsilylmethyl, and the like.

Exemplary organozinc compounds which can be used as co-catalysts can include, but are not limited to, dimethylzinc, diethylzinc, dipropylzinc, dibutylzinc, dineopentylzinc, di(trimethylsilyl)zinc, di(triethylsilyl)zinc, di(triisoproplysilyl)zinc, di(triphenylsilyl)zinc, di(allyldimethylsilyl)zinc, di(trimethylsilylmethyl)zinc, and the like, or combinations thereof.

Similarly, exemplary organomagnesium compounds can include, but are not limited to, dimethylmagnesium, diethylmagnesium, dipropylmagnesium, dibutylmagnesium, dineopentylmagnesium, di(trimethylsilylmethyl)magnesium, methylmagnesium chloride, ethylmagnesium chloride, propylmagnesium chloride, butylmagnesium chloride, neopentylmagnesium chloride, trimethylsilylmethylmagnesium chloride, methylmagnesium bromide, ethylmagnesium bromide, propylmagnesium bromide, butylmagnesium bromide, neopentylmagnesium bromide, trimethylsilylmethylmagnesium bromide, methylmagnesium iodide, ethylmagnesium iodide, propylmagnesium iodide, butylmagnesium iodide, neopentylmagnesium iodide, trimethylsilylmethylmagnesium iodide, methylmagnesium ethoxide, ethylmagnesium ethoxide, propylmagnesium ethoxide, butylmagnesium ethoxide, neopentylmagnesium ethoxide, trimethylsilylmethylmagnesium ethoxide, methylmagnesium propoxide, ethylmagnesium propoxide, propylmagnesium propoxide, butylmagnesium propoxide, neopentylmagnesium propoxide, trimethylsilylmethylmagnesium propoxide, methylmagnesium phenoxide, ethylmagnesium phenoxide, propylmagnesium phenoxide, butylmagnesium phenoxide, neopentylmagnesium phenoxide, trimethylsilylmethylmagnesium phenoxide, and the like, or any combinations thereof.

Likewise, exemplary organolithium compounds can include, but are not limited to, methyllithium, ethyllithium, propyllithium, butyllithium (e.g., t-butyllithium), neopentyllithium, trimethylsilylmethyllithium, phenyllithium, tolyllithium, xylyllithium, benzyllithium, (dimethylphenyl)methyllithium, allyllithium, and the like, or combinations thereof.

Olefin Monomers

Unsaturated reactants that can be employed with catalyst compositions and polymerization processes of this invention typically can include olefin compounds having from 2 to 30 carbon atoms per molecule and having at least one olefinic double bond. This invention encompasses homopolymerization processes using a single olefin such as ethylene or propylene, as well as copolymerization, terpolymerization, etc., reactions using an olefin monomer with at least one different olefinic compound. For example, the resultant ethylene copolymers, terpolymers, etc., generally can contain a major amount of ethylene (>50 mole percent) and a minor amount of comonomer (<50 mole percent), though this is not a requirement. Comonomers that can be copolymerized with ethylene often can have from 3 to 20 carbon atoms, or from 3 to 10 carbon atoms, in their molecular chain.

Acyclic, cyclic, polycyclic, terminal (a), internal, linear, branched, substituted, unsubstituted, functionalized, and non-functionalized olefins can be employed in this invention. For example, typical unsaturated compounds that can be polymerized with the catalyst compositions of this invention can include, but are not limited to, ethylene, propylene, 1-butene, 2-butene, 3-methyl-1-butene, isobutylene, 1-pentene, 2-pentene, 3-methyl-1-pentene, 4-methyl-1-pentene, 1-hexene, 2-hexene, 3-hexene, 3-ethyl-1-hexene, 1-heptene, 2-heptene, 3-heptene, the four normal octenes (e.g., 1-octene), the four normal nonenes, the five normal decenes, and the like, or mixtures of two or more of these compounds. Cyclic and bicyclic olefins, including but not limited to, cyclopentene, cyclohexene, norbornylene, norbornadiene, and the like, also can be polymerized as described herein. Styrene can also be employed as a monomer in the present invention. In an aspect, the olefin monomer can be a C₂-C₂₀ olefin; alternatively, a C₂-C₂₀ α-olefin; alternatively, a C₂-C₁₂ olefin; alternatively, a C₂-C₁₀ α-olefin; alternatively, ethylene, propylene, 1-butene, 1-hexene, or 1-octene; alternatively, ethylene or propylene; alternatively, ethylene; or alternatively, propylene.

When a copolymer (or alternatively, a terpolymer) is desired, the olefin monomer can comprise, for example, ethylene or propylene, which is copolymerized with at least one comonomer (e.g., a C₂-C₂₀ α-olefin, a C₃-C₂₀ α-olefin, etc.). According to one aspect of this invention, the olefin monomer in the polymerization process can comprise ethylene. In this aspect, examples of suitable olefin comonomers can include, but are not limited to, propylene, 1-butene, 2-butene, 3-methyl-1-butene, isobutylene, 1-pentene, 2-pentene, 3-methyl-1-pentene, 4-methyl-1-pentene, 1-hexene, 2-hexene, 3-ethyl-1-hexene, 1-heptene, 2-heptene, 3-heptene, 1-octene, 1-decene, styrene, and the like, or combinations thereof. According to one aspect of the present invention, the comonomer can comprise an α-olefin (e.g., a C₃-C₁₀ α-olefin), while in another embodiment, the comonomer can comprise 1-butene, 1-pentene, 1-hexene, 1-octene, 1-decene, styrene, or any combination thereof. For example, the comonomer can comprise 1-butene, 1-hexene, 1-octene, or a combination thereof.

Generally, the amount of comonomer introduced into a polymerization reactor system to produce a copolymer can be from about 0.01 to about 50 weight percent of the comonomer based on the total weight of the monomer and comonomer. According to another aspect of the present invention, the amount of comonomer introduced into a polymerization reactor system can be from about 0.01 to about 40 weight percent comonomer based on the total weight of the monomer and comonomer. In still another aspect, the amount of comonomer introduced into a polymerization reactor system can be from about 0.1 to about 35 weight percent comonomer based on the total weight of the monomer and comonomer. Yet, in another aspect, the amount of comonomer introduced into a polymerization reactor system can be from about 0.5 to about 20 weight percent comonomer based on the total weight of the monomer and comonomer.

While not intending to be bound by this theory, where branched, substituted, or functionalized olefins are used as reactants, it is believed that a steric hindrance can impede and/or slow the polymerization reaction. Thus, branched and/or cyclic portion(s) of the olefin removed somewhat from the carbon-carbon double bond would not be expected to hinder the reaction in the way that the same olefin substituents situated more proximate to the carbon-carbon double bond might.

According to one aspect of the present invention, at least one monomer/reactant can be ethylene, so the polymerization reaction can be a homopolymerization involving only ethylene, or a copolymerization with a different acyclic, cyclic, terminal, internal, linear, branched, substituted, or unsubstituted olefin. In addition, the catalyst compositions of this invention can be used in the polymerization of diolefin compounds including, but not limited to, 1,3-butadiene, isoprene, 1,4-pentadiene, and 1,5-hexadiene.

Catalyst Compositions

In some aspects, the present invention can employ catalyst compositions containing activator-support I and activator-support II, while in other aspects, the present invention can employ catalyst compositions containing a metallocene compound (one or more than one), activator-support I, and activator-support II. These catalyst compositions can be utilized to produce polyolefins—homopolymers, copolymers, and the like—for a variety of end-use applications. Activator-support I and activator-support II are discussed hereinabove. In aspects of the present invention, it is contemplated that the catalyst composition can contain more than one activator-support I component and/or more than one activator-support II component. Further, additional catalytic compounds—other than those specified as activator-support I, activator-support II, and the metallocene compound—can be employed in the catalyst compositions and/or the polymerization processes, provided that the additional catalytic compound(s) does not detract from the advantages disclosed herein.

The chemically-treated solid oxides of activator-support I are discussed above. For instance, activator-support I can comprise (or consist essentially of, or consist of) a (halided solid oxide) a fluorided solid oxide, a chlorided solid oxide, a bromided solid oxide, an iodided solid oxide, or any combination thereof. The chemically-treated solid oxides of activator-support II also are discussed above. For instance, activator-support II can comprise a sulfated solid oxide, a phosphated solid oxide, or a combination thereof.

Generally, catalyst compositions of the present invention comprise a metallocene compound, activator-support I, and activator-support II. Various bridged, unbridged, and dinuclear metallocene compounds useful in the present invention are disclosed hereinabove. Optionally, such catalyst compositions can further comprise one or more than one co-catalyst compound or compounds (suitable co-catalysts, such as organoaluminum compounds, also are discussed hereinabove). Thus, a catalyst composition of this invention can comprise a metallocene compound, activator-support I, activator-support II, and an organoaluminum compound. For instance, activator-support I can comprise (or consist essentially of, or consist of) fluorided alumina, chlorided alumina, fluorided silica-alumina, chlorided silica-alumina, fluorided silica-coated alumina, chlorided silica-coated alumina, or combinations thereof. Likewise, activator-support II can comprise (or consist essentially of, or consist of) sulfated alumina, phosphated alumina, sulfated silica-alumina, phosphated silica-alumina, sulfated silica-coated alumina, phosphated silica-coated alumina, or combinations thereof. Additionally, the organoaluminum compound can comprise (or consist essentially of, or consist of) trimethylaluminum, triethylaluminum, tri-n-propylaluminum, tri-n-butylaluminum, triisobutylaluminum, tri-n-hexylaluminum, tri-n-octylaluminum, diisobutylaluminum hydride, diethylaluminum ethoxide, diethylaluminum chloride, and the like, or combinations thereof. Accordingly, a catalyst composition consistent with aspects of the invention can comprise (or consist essentially of, or consist of) an unbridged zirconium or hafnium based metallocene compound; or a bridged zirconium or hafnium based metallocene compound with a fluorenyl group, and with no aryl groups on the bridging group; or a bridged zirconium or hafnium based metallocene compound with a fluorenyl group, and an aryl group on the bridging group; and a fluorided solid oxide (or chlorided solid oxide); and a sulfated solid oxide (or a phosphated solid oxide); and a co-catalyst (or an organoaluminum compound, such as triethylaluminum or triisobutylaluminum).

In another aspect of the present invention, a catalyst composition is provided which comprises a metallocene compound, activator-support I, and activator-support II (with or without a co-catalyst), wherein this catalyst composition is substantially free of aluminoxanes, organoboron or organoborate compounds, ionizing ionic compounds, and/or other similar materials; alternatively, substantially free of aluminoxanes; alternatively, substantially free or organoboron or organoborate compounds; or alternatively, substantially free of ionizing ionic compounds. In these aspects, the catalyst composition has catalyst activity, discussed herein below, in the absence of these additional materials. For example, a catalyst composition of the present invention can consist essentially of a metallocene compound, activator-support I, and activator-support II (or a metallocene compound, activator-support I, activator-support II, and an organoaluminum compound), wherein no other materials are present in the catalyst composition which would increase/decrease the activity of the catalyst composition by more than about 10% from the catalyst activity of the catalyst composition in the absence of said materials.

However, in other aspects of this invention, these co-catalysts can be employed. For example, a catalyst composition containing a metallocene compound, activator-support I, and activator-support II, can further comprise an optional co-catalyst. Suitable co-catalysts in this aspect can include, but are not limited to, aluminoxane compounds, organoboron or organoborate compounds, ionizing ionic compounds, organoaluminum compounds, organozinc compounds, organomagnesium compounds, organolithium compounds, and the like, or any combination thereof; or alternatively, organoaluminum compounds, organozinc compounds, organomagnesium compounds, organolithium compounds, or any combination thereof. More than one co-catalyst can be present in the catalyst composition.

In a particular aspect contemplated herein, the catalyst composition is a catalyst composition comprising a metallocene compound (one or more than one), only one activator-support I component, and only one activator-support II component. In these and other aspects, the catalyst composition can comprise a metallocene compound; fluorided alumina, chlorided alumina, fluorided silica-alumina, chlorided silica-alumina, fluorided silica-coated alumina, or chlorided silica-coated alumina; and sulfated alumina, phosphated alumina, sulfated silica-alumina, phosphated silica-alumina, sulfated silica-coated alumina, or phosphated silica-coated alumina.

This invention further encompasses methods of making these catalyst compositions, such as, for example, contacting the respective catalyst components in any order or sequence. Hence, in one aspect, the catalyst composition can be produced by a process comprising contacting, in any order, the metallocene compound, activator-support I, and activator-support II. In another aspect, the catalyst composition can be produced by a process comprising contacting, in any order, the metallocene compound, activator-support I, activator-support II, and the co-catalyst (e.g., an organoaluminum compound).

The metallocene compound can be precontacted with an olefinic monomer if desired, not necessarily the olefin monomer to be polymerized, and an organoaluminum compound for a first period of time prior to contacting this precontacted mixture with the activator-supports. The first period of time for contact, the precontact time, between the metallocene compound, the olefinic monomer, and the organoaluminum compound typically ranges from a time period of about 1 minute to about 24 hours, for example, from about 3 minutes to about 1 hour. Precontact times from about 10 minutes to about 30 minutes also can be employed. Alternatively, the precontacting process can be carried out in multiple steps, rather than a single step, in which multiple mixtures can be prepared, each comprising a different set of catalyst components. For example, at least two catalyst components can be contacted forming a first mixture, followed by contacting the first mixture with at least one other catalyst component forming a second mixture, and so forth.

Multiple precontacting steps can be carried out in a single vessel or in multiple vessels. Further, multiple precontacting steps can be carried out in series (sequentially), in parallel, or a combination thereof. For example, a first mixture of two catalyst components can be formed in a first vessel, a second mixture comprising the first mixture plus one additional catalyst component can be formed in the first vessel or in a second vessel, which is typically placed downstream of the first vessel.

In another aspect, one or more of the catalyst components can be split and used in different precontacting treatments. For example, part of a catalyst component can be fed into a first precontacting vessel for precontacting with at least one other catalyst component, while the remainder of that same catalyst component can be fed into a second precontacting vessel for precontacting with at least one other catalyst component, or can be fed directly into the reactor, or a combination thereof. The precontacting can be carried out in any suitable equipment, such as tanks, stirred mix tanks, various static mixing devices, a flask, a vessel of any type, or combinations of these apparatus.

In another aspect of this invention, the various catalyst components (for example, a metallocene compound, activator-support I, and activator-support II, an organoaluminum co-catalyst, and optionally an unsaturated hydrocarbon) can be contacted in the polymerization reactor simultaneously while the polymerization reaction is proceeding. Alternatively, any two or more of these catalyst components can be precontacted in a vessel prior to entering the reaction zone. This precontacting step can be continuous, in which the precontacted product can be fed continuously to the reactor, or it can be a stepwise or batchwise process in which a batch of precontacted product can be added to make a catalyst composition. This precontacting step can be carried out over a time period that can range from a few seconds to as much as several days, or longer. In this aspect, the continuous precontacting step generally can last from about 1 second to about 1 hour. In another aspect, the continuous precontacting step can last from about 10 seconds to about 45 minutes, or from about 1 minute to about 30 minutes.

Once the precontacted mixture of metallocene compound, the olefin monomer, and the organoaluminum co-catalyst is contacted with the activator-supports, this composition (with the addition of the activator-supports) can be termed the “postcontacted mixture.” The postcontacted mixture optionally can remain in contact for a second period of time, the postcontact time, prior to initiating the polymerization process. Postcontact times between the precontacted mixture and the activator-support generally range from about 1 minute to about 24 hours. In a further aspect, the postcontact time can be in a range from about 3 minutes to about 1 hour. The precontacting step, the postcontacting step, or both, can increase the productivity of the polymer as compared to the same catalyst composition that is prepared without precontacting or postcontacting. However, neither a precontacting step nor a postcontacting step is required.

The postcontacted mixture can be heated at a temperature and for a time period sufficient to allow adsorption, impregnation, or interaction of precontacted mixture and the activator-supports, such that a portion of the components of the precontacted mixture can be immobilized, adsorbed, or deposited thereon. Where heating is employed, the postcontacted mixture generally can be heated to a temperature of from between about 0° F. to about 150° F., or from about 40° F. to about 95° F.

When a precontacting step is used, the molar ratio of the total moles of olefin monomer to total moles of metallocene(s) in the precontacted mixture typically can be in a range from about 1:10 to about 100,000:1. Total moles of each component are used in this ratio to account for aspects of this invention where more than one olefin monomer and/or more than one metallocene compound is employed in a precontacting step. Further, this molar ratio can be in a range from about 10:1 to about 1,000:1 in another aspect of the invention.

Generally, the weight ratio of organoaluminum compound to activator-supports can be in a range from about 10:1 to about 1:1000. If more than one organoaluminum compound is employed, this ratio is based on the total weight of each respective component. In another aspect, the weight ratio of the organoaluminum compound to the activator-supports can be in a range from about 3:1 to about 1:100, or from about 1:1 to about 1:50.

In some aspects of this invention, the weight ratio of metallocene compound to activator-support (total of activator-support I and activator-support II) can be in a range from about 1:1 to about 1:1,000,000. In another aspect, this weight ratio can be in a range from about 1:5 to about 1:100,000, or from about 1:10 to about 1:10,000. Yet, in another aspect, the weight ratio of the metallocene compound to the activator-supports can be in a range from about 1:20 to about 1:1000.

Catalyst compositions of the present invention generally have a catalyst activity greater than about 100 grams of polyethylene (homopolymer, copolymer, etc., as the context requires) per gram of activator-supports per hour (abbreviated g/g/hr). In another aspect, the catalyst activity can be greater than about 150, greater than about 250, or greater than about 500 g/g/hr. In still another aspect, catalyst compositions of this invention can be characterized by having a catalyst activity greater than about 550, greater than about 650, or greater than about 750 g/g/hr. Yet, in another aspect, the catalyst activity can be greater than about 1000 g/g/hr, or greater than about 1500 g/g/hr. These activities are measured under slurry polymerization conditions using isobutane as the diluent, at a polymerization temperature of about 80° C. and a reactor pressure of about 310 psig. Moreover, such catalyst activities can be achieved when the catalyst composition contains a co-catalyst, such as an organoaluminum compound (e.g., triethylaluminum, triisobutylaluminum, etc.). Additionally, in some aspects, activator-support I can comprise fluorided alumina, fluorided silica-alumina, or fluorided silica-coated alumina, and activator-support II can comprise sulfated alumina, phosphated alumina, sulfated silica-alumina, phosphated silica-alumina, sulfated silica-coated alumina, or phosphated silica-coated alumina.

As discussed hereinabove, any combination of the metallocene compound, activator-support I, activator-support II, the organoaluminum compound, and the olefin monomer, can be precontacted in some aspects of this invention. When any precontacting occurs with an olefinic monomer, it is not necessary that the olefin monomer used in the precontacting step be the same as the olefin to be polymerized. Further, when a precontacting step among any combination of the catalyst components is employed for a first period of time, this precontacted mixture can be used in a subsequent postcontacting step between any other combination of catalyst components for a second period of time. For example, one or more metallocene compounds, the organoaluminum compound, and 1-hexene can be used in a precontacting step for a first period of time, and this precontacted mixture then can be contacted with the activator-supports to form a postcontacted mixture that can be contacted for a second period of time prior to initiating the polymerization reaction. For example, the first period of time for contact, the precontact time, between any combination of the metallocene compound, the olefinic monomer, the activator-supports, and the organoaluminum compound can be from about 1 minute to about 24 hours, from about 3 minutes to about 1 hour, or from about 10 minutes to about 30 minutes. The postcontacted mixture optionally can be allowed to remain in contact for a second period of time, the postcontact time, prior to initiating the polymerization process. According to one aspect of this invention, postcontact times between the precontacted mixture and any remaining catalyst components can be from about 1 minute to about 24 hours, or from about 5 minutes to about 1 hour.

Polymerization Processes

Catalyst compositions of the present invention can be used to polymerize olefins to form homopolymers, copolymers, terpolymers, and the like. One such process for polymerizing olefins in the presence of a catalyst composition of the present invention can comprise contacting the catalyst composition with an olefin monomer and optionally an olefin comonomer (one or more) in a polymerization reactor system under polymerization conditions to produce an olefin polymer, wherein the catalyst composition can comprise a metallocene compound, activator-support I, activator-support II, and an optional co-catalyst. Activator-supports I and II, and suitable bridged, unbridged, and/or dinuclear metallocene compounds, are discussed hereinabove. The catalyst composition, optionally, can further comprise one or more than one organoaluminum compound or compounds (or other suitable co-catalyst). Thus, a process for polymerizing olefins in the presence of a catalyst composition can employ a catalyst composition comprising a metallocene compound (one or more), activator-support I, activator-support II, and an organoaluminum compound.

In some aspects, activator-support I can comprise (or consist essentially of, or consist of) fluorided alumina, chlorided alumina, fluorided silica-alumina, chlorided silica-alumina, fluorided silica-coated alumina, chlorided silica-coated alumina, or any combination thereof, while activator-support II can comprise (or consist essentially of, or consist of) sulfated alumina, phosphated alumina, sulfated silica-alumina, phosphated silica-alumina, sulfated silica-coated alumina, phosphated silica-coated alumina, or any combination thereof. In some aspects, the organoaluminum compound can comprise (or consist essentially of, or consist of) trimethylaluminum, triethylaluminum, tri-n-propylaluminum, tri-n-butylaluminum, triisobutylaluminum, tri-n-hexylaluminum, tri-n-octylaluminum, diisobutylaluminum hydride, diethylaluminum ethoxide, diethylaluminum chloride, and the like, or combinations thereof.

In accordance with another aspect of the invention, the polymerization process can employ a catalyst composition comprising a metallocene compound, activator-support I, activator-support II, and an optional co-catalyst, wherein the co-catalyst can comprise an aluminoxane compound, an organoboron or organoborate compound, an ionizing ionic compound, an organoaluminum compound, an organozinc compound, an organomagnesium compound, or an organolithium compound, or any combination thereof. Hence, aspects of this invention are directed to a process for polymerizing olefins in the presence of a catalyst composition, the processes comprising contacting a catalyst composition with an olefin monomer and optionally an olefin comonomer (one or more) under polymerization conditions to produce an olefin polymer, and the catalyst composition can comprise a metallocene compound, activator-support I, activator-support II, and an aluminoxane compound; alternatively, a metallocene compound, activator-support I, activator-support II, and an organoboron or organoborate compound; alternatively, a metallocene compound, activator-support I, activator-support II, and an ionizing ionic compound; alternatively, a metallocene compound, activator-support I, activator-support II, and an organoaluminum compound; alternatively, a metallocene compound, activator-support I, activator-support II, and an organozinc compound; alternatively, a metallocene compound, activator-support I, activator-support II, and an organomagnesium compound; or alternatively, a metallocene compound, activator-support I, activator-support II, and an organolithium compound. Furthermore, more than one co-catalyst can be employed, e.g., an organoaluminum compound and an aluminoxane compound, an organoaluminum compound and an ionizing ionic compound, etc.

In accordance with another aspect of the invention, the polymerization process can employ a catalyst composition comprising a metallocene compound, only one activator-support I component, only one activator-support II component, and a co-catalyst, such as an organoaluminum compound.

The catalyst compositions of the present invention are intended for any olefin polymerization method using various types of polymerization reactor systems and reactors. The polymerization reactor system can include any polymerization reactor capable of polymerizing olefin monomers and comonomers (one or more than one comonomer) to produce homopolymers, copolymers, terpolymers, and the like. The various types of reactors include those that can be referred to as a batch reactor, slurry reactor, gas-phase reactor, solution reactor, high pressure reactor, tubular reactor, autoclave reactor, and the like, or combinations thereof. Suitable polymerization conditions are used for the various reactor types. Gas phase reactors can comprise fluidized bed reactors or staged horizontal reactors. Slurry reactors can comprise vertical or horizontal loops. High pressure reactors can comprise autoclave or tubular reactors. Reactor types can include batch or continuous processes. Continuous processes could use intermittent or continuous product discharge. Processes can also include partial or full direct recycle of unreacted monomer, unreacted comonomer, and/or diluent.

Polymerization reactor systems of the present invention can comprise one type of reactor in a system or multiple reactors of the same or different type (e.g., a single reactor, dual reactor, more than two reactors). Production of polymers in multiple reactors can include several stages in at least two separate polymerization reactors interconnected by a transfer device making it possible to transfer the polymers resulting from the first polymerization reactor into the second reactor. The desired polymerization conditions in one of the reactors can be different from the operating conditions of the other reactor(s). Alternatively, polymerization in multiple reactors can include the manual transfer of polymer from one reactor to subsequent reactors for continued polymerization. Multiple reactor systems can include any combination including, but not limited to, multiple loop reactors, multiple gas phase reactors, a combination of loop and gas phase reactors, multiple high pressure reactors, or a combination of high pressure with loop and/or gas phase reactors. The multiple reactors can be operated in series, in parallel, or both.

According to one aspect of the invention, the polymerization reactor system can comprise at least one loop slurry reactor comprising vertical or horizontal loops. Monomer, diluent, catalyst, and comonomer can be continuously fed to a loop reactor where polymerization occurs. Generally, continuous processes can comprise the continuous introduction of monomer/comonomer, a catalyst system, and a diluent into a polymerization reactor and the continuous removal from this reactor of a suspension comprising polymer particles and the diluent. Reactor effluent can be flashed to remove the solid polymer from the liquids that comprise the diluent, monomer and/or comonomer. Various technologies can be used for this separation step including but not limited to, flashing that can include any combination of heat addition and pressure reduction, separation by cyclonic action in either a cyclone or hydrocyclone, or separation by centrifugation.

A typical slurry polymerization process (also known as the particle form process) is disclosed, for example, in U.S. Pat. Nos. 3,248,179, 4,501,885, 5,565,175, 5,575,979, 6,239,235, 6,262,191, and 6,833,415, each of which is incorporated herein by reference in its entirety.

Suitable diluents used in slurry polymerization include, but are not limited to, the monomer being polymerized and hydrocarbons that are liquids under reaction conditions. Examples of suitable diluents include, but are not limited to, hydrocarbons such as propane, cyclohexane, isobutane, n-butane, n-pentane, isopentane, neopentane, and n-hexane. Some loop polymerization reactions can occur under bulk conditions where no diluent is used. An example is polymerization of propylene monomer as disclosed in U.S. Pat. No. 5,455,314, which is incorporated by reference herein in its entirety.

According to yet another aspect of this invention, the polymerization reactor system can comprise at least one gas phase reactor. Such systems can employ a continuous recycle stream containing one or more monomers continuously cycled through a fluidized bed in the presence of the catalyst under polymerization conditions. A recycle stream can be withdrawn from the fluidized bed and recycled back into the reactor. Simultaneously, polymer product can be withdrawn from the reactor and new or fresh monomer can be added to replace the polymerized monomer. Such gas phase reactors can comprise a process for multi-step gas-phase polymerization of olefins, in which olefins are polymerized in the gaseous phase in at least two independent gas-phase polymerization zones while feeding a catalyst-containing polymer formed in a first polymerization zone to a second polymerization zone. One type of gas phase reactor is disclosed in U.S. Pat. Nos. 5,352,749, 4,588,790, and 5,436,304, each of which is incorporated by reference in its entirety herein.

According to still another aspect of the invention, a high pressure polymerization reactor system can comprise a tubular reactor or an autoclave reactor. Tubular reactors can have several zones where fresh monomer, initiators, or catalysts are added. Monomer can be entrained in an inert gaseous stream and introduced at one zone of the reactor. Initiators, catalysts, and/or catalyst components can be entrained in a gaseous stream and introduced at another zone of the reactor. The gas streams can be intermixed for polymerization. Heat and pressure can be employed appropriately to obtain optimal polymerization reaction conditions.

According to yet another aspect of the invention, the polymerization reactor system can comprise a solution polymerization reactor wherein the monomer (and comonomer, if used) are contacted with the catalyst composition by suitable stirring or other means. A carrier comprising an inert organic diluent or excess monomer can be employed. If desired, the monomer/comonomer can be brought in the vapor phase into contact with the catalytic reaction product, in the presence or absence of liquid material. The polymerization zone is maintained at temperatures and pressures that will result in the formation of a solution of the polymer in a reaction medium. Agitation can be employed to obtain better temperature control and to maintain uniform polymerization mixtures throughout the polymerization zone. Adequate means are utilized for dissipating the exothermic heat of polymerization.

Polymerization reactor systems suitable for the present invention can further comprise any combination of at least one raw material feed system, at least one feed system for catalyst or catalyst components, and/or at least one polymer recovery system. Suitable reactor systems for the present invention can further comprise systems for feedstock purification, catalyst storage and preparation, extrusion, reactor cooling, polymer recovery, fractionation, recycle, storage, loadout, laboratory analysis, and process control.

Polymerization conditions that are controlled for efficiency and to provide desired polymer properties can include temperature, pressure, and the concentrations of various reactants. Polymerization temperature can affect catalyst productivity, polymer molecular weight, and molecular weight distribution. A suitable polymerization temperature can be any temperature below the de-polymerization temperature according to the Gibbs Free energy equation. Typically, this includes from about 60° C. to about 280° C., for example, or from about 60° C. to about 120° C., depending upon the type of polymerization reactor(s). In some reactor systems, the polymerization temperature generally can fall within a range from about 70° C. to about 100° C., or from about 75° C. to about 95° C. Various polymerization conditions can be held substantially constant, for example, for the production of a particular grade of olefin polymer.

Suitable pressures will also vary according to the reactor and polymerization type. The pressure for liquid phase polymerizations in a loop reactor is typically less than 1000 psig (6.9 MPa). Pressure for gas phase polymerization is usually at about 200 to 500 psig (1.4 MPa to 3.4 MPa). High pressure polymerization in tubular or autoclave reactors is generally run at about 20,000 to 75,000 psig (138 to 517 MPa). Polymerization reactors can also be operated in a supercritical region occurring at generally higher temperatures and pressures. Operation above the critical point of a pressure/temperature diagram (supercritical phase) may offer advantages.

Aspects of this invention are directed to olefin polymerization processes comprising contacting a catalyst composition with an olefin monomer and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce an olefin polymer. The olefin polymer (e.g., an ethylene copolymer) produced by the process can have any of the polymer properties disclosed herein, for example, a melt index of less than or equal to about 25 g/10 min, a density in a range from about 0.89 g/cm³ to about 0.96 g/cm³, a Mw in a range from about 75,000 to about 500,000 g/mol, and/or a Mn in a range from about 5,000 to about 150,000 g/mol.

Aspects of this invention also are directed to olefin polymerization processes conducted in the absence of added hydrogen. An olefin polymerization process of this invention can comprise contacting a catalyst composition with an olefin monomer and optionally an olefin comonomer in a polymerization reactor system under polymerization conditions to produce an olefin polymer, wherein the catalyst composition can comprise a metallocene compound, activator-support I, activator-support II, and an optional co-catalyst, wherein the polymerization process is conducted in the absence of added hydrogen (no hydrogen is added to the polymerization reactor system). As one of ordinary skill in the art would recognize, hydrogen can be generated in-situ by metallocene catalyst compositions in various olefin polymerization processes, and the amount generated can vary depending upon the specific catalyst composition and metallocene compound(s) employed, the type of polymerization process used, the polymerization reaction conditions utilized, and so forth.

In other aspects, it may be desirable to conduct the polymerization process in the presence of a certain amount of added hydrogen. Accordingly, an olefin polymerization process of this invention can comprise contacting a catalyst composition with an olefin monomer and optionally an olefin comonomer in a polymerization reactor system under polymerization conditions to produce an olefin polymer, wherein the catalyst composition comprises a metallocene compound, activator-support I, activator-support II, and an optional co-catalyst, wherein the polymerization process is conducted in the presence of added hydrogen (hydrogen is added to the polymerization reactor system). For example, the ratio of hydrogen to the olefin monomer in the polymerization process can be controlled, often by the feed ratio of hydrogen to the olefin monomer entering the reactor. The added hydrogen to olefin monomer ratio in the process can be controlled, for instance, at a weight ratio which falls within a range from about 25 ppm to about 1500 ppm, from about 50 to about 1000 ppm, or from about 100 ppm to about 750 ppm.

In some aspects of this invention, the feed or reactant ratio of hydrogen to olefin monomer can be maintained substantially constant during the polymerization run for a particular polymer grade. That is, the hydrogen:olefin monomer ratio can be selected at a particular ratio within a range from about 5 ppm up to about 1000 ppm or so, and maintained at the ratio to within about +/−25% during the polymerization run. For instance, if the target ratio is 100 ppm, then maintaining the hydrogen:olefin monomer ratio substantially constant would entail maintaining the feed ratio between about 75 ppm and about 125 ppm. Further, the addition of comonomer (or comonomers) can be, and generally is, substantially constant throughout the polymerization run for a particular polymer grade.

However, in other aspects, it is contemplated that monomer, comonomer (or comonomers), and/or hydrogen can be periodically pulsed to the reactor, for instance, in a manner similar to that employed in U.S. Pat. No. 5,739,220 and U.S. Patent Publication No. 2004/0059070, the disclosures of which are incorporated herein by reference in their entirety.

Processes of the present invention which utilize a catalyst composition comprising a metallocene compound, activator-support I, activator-support II, and an optional co-catalyst, unexpectedly, can result in an olefin polymer having a greater molecular weight parameter (e.g., Mn, Mw, etc.) than that of an olefin polymer obtained under the same polymerization conditions without activator-support I in the catalyst composition, and than that of an olefin polymer obtained under the same polymerization conditions without activator-support II in the catalyst composition. While not wishing to be bound by theory, Applicants believe that a catalyst system having both a halogenated solid oxide and either a sulfated solid oxide or a phosphated solid oxide (or both) can result in higher molecular weights under the same conditions than catalyst systems containing only one of the chemically treated solid oxides alone. As described herein, “same polymerization conditions” means include identical polymerization conditions (e.g., temperature, pressure, catalyst productivity or catalyst activity, etc.) and identical materials (e.g., metallocene compound, co-catalyst, total weight of activator-support(s), etc.), with the exception of the selection of the activator-supports. As an example, a catalyst system in accordance with the present invention can contain 100 mg of fluorided alumina as activator-support I, and 100 mg of sulfated alumina as activator-support II. A molecular weight parameter (e.g., Mw) of the olefin polymer (e.g., an ethylene copolymer) produced by the polymerization process using a catalyst system containing a metallocene compound, 100 mg of fluorided alumina, and 100 mg of sulfated alumina, can be greater than the same molecular weight parameter of an olefin polymer obtained under the same polymerization conditions with either 200 mg of fluorided alumina or 200 mg of sulfated alumina in the catalyst system.

The processes disclosed herein, utilizing the above-described dual activator-support catalyst systems, can result in an olefin polymer having an increased molecular weight parameter, for instance, an increased weight-average molecular weight (Mw). In some aspects, the Mw of the olefin polymer produced by the process (using a dual activator-support catalyst system) can be at least 1% greater, at least 2% greater, at least 3% greater, at least 4% greater, or at least 5% greater, than a Mw of an olefin polymer obtained under the same polymerization conditions without activator-support I or without activator-support II (i.e., a single activator-support catalyst system). For instance, the Mw of the olefin polymer produced by the process can be from 1% to about 25% greater, from 1% to about 20% greater, from about 2% to about 20% greater, or from about 3% to about 20% greater, than the Mw of the olefin polymer obtained under the same polymerization conditions without activator-support I or without activator-support II.

The processes disclosed herein, utilizing the above-described dual activator-support catalyst systems, can result in an olefin polymer having an increased molecular weight parameter, for instance, an increased number-average molecular weight (Mn). In some aspects, the Mn of the olefin polymer produced by the process (using a dual activator-support catalyst system) can be at least 1% greater, at least 2% greater, at least 3% greater, at least 4% greater, or at least 5% greater, than a Mn of an olefin polymer obtained under the same polymerization conditions without activator-support I or without activator-support II (i.e., a single activator-support catalyst system). For instance, the Mn of the olefin polymer produced by the process can be from 1% to about 25% greater, from 1% to about 20% greater, from about 2% to about 20% greater, or from about 3% to about 20% greater, than the Mn of the olefin polymer obtained under the same polymerization conditions without activator-support I or without activator-support II.

The concentration of the reactants entering the polymerization reactor system can be controlled to produce resins with certain physical and mechanical properties. The proposed end-use product that will be formed by the polymer resin and the method of forming that product ultimately can determine the desired polymer properties and attributes. Mechanical properties include tensile, flexural, impact, creep, stress relaxation, and hardness tests. Physical properties include density, molecular weight, molecular weight distribution, melting temperature, glass transition temperature, temperature melt of crystallization, density, stereoregularity, crack growth, long chain branching, and rheological measurements.

This invention is also directed to, and encompasses, the polymers produced by any of the polymerization processes disclosed herein. Articles of manufacture can be formed from, and/or can comprise, the polymers produced in accordance with this invention.

Polymers and Articles

Olefin polymers encompassed herein can include any polymer produced from any olefin monomer and optional comonomer(s) described herein. For example, the olefin polymer can comprise an ethylene homopolymer, a propylene homopolymer, an ethylene copolymer (e.g., ethylene/α-olefin, ethylene/1-butene, ethylene/1-hexene, ethylene/1-octene, etc.), a propylene copolymer, an ethylene terpolymer, a propylene terpolymer, and the like, including combinations thereof. In one aspect, the olefin polymer can be an ethylene/1-butene copolymer, an ethylene/1-hexene copolymer, or an ethylene/1-octene copolymer, while in another aspect, the olefin polymer can be an ethylene/1-hexene copolymer.

If the resultant polymer produced in accordance with the present invention is, for example, an ethylene polymer, its properties can be characterized by various analytical techniques known and used in the polyolefin industry. Articles of manufacture can be formed from, and/or can comprise, the olefin polymers (e.g., ethylene polymers) of this invention, whose typical properties are provided below.

Polymers of ethylene (homopolymers, copolymers, terpolymers, etc.) produced in accordance with some aspects of this invention generally can have a melt index (MI, g/10 min, ASTM D1238, 190° C. and 2,160 gram weight) from 0 to about 25 g/10 min. Melt indices in the range from 0 to about 10 g/10 min, from 0 to about 5 g/10 min, from 0 to about 2 g/10 min, or from 0 to about 1 g/10 min, are contemplated in other aspects of this invention. For example, a polymer of the present invention can have a melt index in a range from about 0.01 to about 25, from about 0.1 to about 25, from about 0.5 to about 25, from about 0.1 to about 10, from about 0.1 to about 3, from about 0.5 to about 3, or from about 0.5 to about 1.5 g/10 min.

The densities of ethylene-based polymers produced using the catalyst systems and processes disclosed herein often are greater than or equal to about 0.89 g/cm³ (ASTM D1505 and ASTM D1928, procedure C). In one aspect of this invention, the density of the ethylene polymer can be in a range from about 0.89 to about 0.96 g/cm³. Yet, in another aspect, the density can be in a range from about 0.91 to about 0.96 g/cm³, such as, for example, from about 0.91 to about 0.95 g/cm³, from about 0.91 to about 0.94 g/cm³, or from about 0.91 to about 0.93 g/cm³.

Ethylene polymers, such as copolymers, terpolymers, etc., consistent with various aspects of the present invention generally can have weight-average molecular weights (Mw's), for instance, in a range from about 50,000 to about 700,000 g/mol, from about 75,000 to about 500,000 g/mol, from about 100,000 to about 500,000 g/mol, from about 100,000 to about 400,000 g/mol, or from about 150,000 to about 600,000 g/mol. Likewise, suitable non-limiting ranges of the number-average molecular weight (Mn) can include, but are not limited to, from about 5,000 to about 150,000 g/mol, from about 5,000 to about 50,000 g/mol, from about 10,000 to about 150,000 g/mol, from about 10,000 to about 50,000 g/mol, or from about 50,000 to about 150,000 g/mol.

The ratio of Mw/Mn, or the polydispersity index, for the polymers of this invention are not limited to any particular range. In some aspects, however, the ratio of Mw/Mn can be in a range from about 2 to about 40, from about 2.2 to about 35, from about 2.2 to about 30, from about 2.4 to about 30, from about 2 to about 25, from about 2.2 to about 10, from about 2.2 to about 5, from about 2 to about 4, from about 2.2 to about 3, from about 2.4 to about 3.5, or from about 10 to about 40.

Polymers of ethylene, whether homopolymers, copolymers, and so forth, can be formed into various articles of manufacture. Articles which can comprise polymers of this invention include, but are not limited to, an agricultural film, an automobile part, a bottle, a drum, a fiber or fabric, a food packaging film or container, a food service article, a fuel tank, a geomembrane, a household container, a liner, a molded product, a medical device or material, a pipe, a sheet or tape, a toy, and the like. Various processes can be employed to form these articles. Non-limiting examples of these processes include injection molding, blow molding, rotational molding, film extrusion, sheet extrusion, profile extrusion, thermoforming, and the like. Additionally, additives and modifiers are often added to these polymers in order to provide beneficial polymer processing or end-use product attributes. Such processes and materials are described in Modern Plastics Encyclopedia, Mid-November 1995 Issue, Vol. 72, No. 12; and Film Extrusion Manual—Process, Materials, Properties, TAPPI Press, 1992; the disclosures of which are incorporated herein by reference in their entirety.

Applicants also contemplate a method for forming or preparing an article of manufacture comprising a polymer produced by any of the polymerization processes disclosed herein. For instance, a method can comprise (i) contacting a catalyst composition with an olefin monomer and an optional olefin comonomer in a polymerization reaction system under polymerization conditions to produce an olefin polymer, wherein the catalyst composition can comprise a metallocene compound, activator-support I (e.g., a fluorided solid oxide), activator-support II (e.g., a sulfated solid oxide), and an optional co-catalyst (e.g., an organoaluminum compound); and (ii) forming an article of manufacture comprising the olefin polymer. The forming step can comprise blending, melt processing, extruding, molding, or thermoforming, and the like, including combinations thereof.

EXAMPLES

The invention is further illustrated by the following examples, which are not to be construed in any way as imposing limitations to the scope of this invention. Various other aspects, embodiments, modifications, and equivalents thereof which, after reading the description herein, may suggest themselves to one of ordinary skill in the art without departing from the spirit of the present invention or the scope of the appended claims.

The following representative bridged and unbridged metallocene compounds were used in the examples that follow (Me=methyl; t-Bu=tert-butyl):

Molecular weights and molecular weight distributions were obtained using a PL-GPC 220 (Polymer Labs, an Agilent Company) system equipped with a IR4 detector (Polymer Char, Spain) and three Styragel HMW-6E GPC columns (Waters, MA) running at 145° C. The flow rate of the mobile phase 1,2,4-trichlorobenzene (TCB) containing 0.5 g/L 2,6-di-t-butyl-4-methylphenol (BHT) was set at 1 mL/min, and polymer solution concentrations were in the range of 1.0-1.5 mg/mL, depending on the molecular weight. Sample preparation was conducted at 150° C. for nominally 4 hr with occasional and gentle agitation, before the solutions were transferred to sample vials for injection. The integral calibration method was used to deduce molecular weights and molecular weight distributions using a Chevron Phillips Chemicals Company's HDPE polyethylene resin, MARLEX® BHB5003, as the standard. The integral table of the standard was pre-determined in a separate experiment with SEC-MALS. To minimize variation, Examples 1-5 were analyzed at the same time, and Examples 6-10 were analyzed at the same time.

An alumina was obtained from W.R. Grace under the designation “Alumina A” having a surface area of about 300 m²/g and a pore volume of about 1.2 mL/g. This material was obtained as a powder having an average particle size of about 90 microns. The alumina was first calcined at about 600° C. for approximately 6 hours, and then contacted with tetraethylorthosilicate in isopropanol to equal 25% SiO₂. After drying, the solid oxide was impregnated to incipient wetness with 10% ammonium bifluoride (based on the weight of the solid oxide) in solution in methanol. This mixture was then placed in a flat pan and allowed to dry under vacuum at approximately 110° C. for about 16 hours. To calcine the support, about 10 grams of this powdered mixture were placed in a 1.75-inch quartz tube fitted with a sintered quartz disk at the bottom. While the powder was supported on the disk, air (nitrogen can be substituted) dried by passing through a 13× molecular sieve column, was blown upward through the disk at the linear rate of about 1.6 to 1.8 standard cubic feet per hour. An electric furnace around the quartz tube was then turned on and the temperature was raised at the rate of about 400° C. per hour to the desired calcining temperature of about 600° C. At this temperature, the powder was allowed to fluidize for about three hours in the dry air. Afterward, the fluorided silica-coated alumina was collected and stored under dry nitrogen, and was used without exposure to the atmosphere. This fluorided silica-coated alumina activator-support is abbreviated F—Si/Al in the examples that follow.

The sulfated alumina activator-support was prepared from the same alumina (Alumina A from W.R. Grace) used for the fluorided silica-coated alumina. After being calcined in a muffle furnace for 12 hours at 600° C., the alumina was allowed to cool. Then, the solid oxide was impregnated with a solution of sulfuric acid in methanol, such that 3 mL of methanol were added per gram of alumina. The methanol contained enough sulfuric acid to equal about 15% sulfate based on the weight of the alumina. The sulfated alumina was then calcined as described for the fluorided silica-coated alumina. The resulting sulfated alumina activator-support is abbreviated S—Al in the examples that follow.

Examples 1-5

Examples 1-5 were produced using the following polymerization procedure. All polymerization runs were conducted in a one-gallon stainless steel reactor with 1.8 L of isobutane. A metallocene solution of MET-A was prepared at about 1 mg/mL in toluene. Approximately 0.4 mmol of alkyl aluminum (triisobutylaluminum), 100 mg total of activator-support(s), and 2 mg of MET-A were added in that order through a charge port while slowly venting isobutane vapor. The charge port was closed and isobutane was added. The contents of the reactor were stirred and heated to the desired run temperature of about 80° C., and ethylene was then introduced into the reactor. Ethylene was fed on demand to maintain the target pressure of 310 psig pressure for the length of the polymerization run, which was varied to maintain comparable catalyst productivity or polymer production to within +/−5% of 270 grams for Examples 1-5. The reactor was maintained at the desired temperature throughout the run by an automated heating-cooling system.

Table I summarizes the activator-supports used in Examples 1-5 and the molecular weight properties of the polymers of Examples 1-5 (these homopolymers had melt index values of zero). In Table I, Mn is the number-average molecular weight, and Mw is the weight-average molecular weight. Unexpectedly, the polymers produced using both a fluorided solid oxide and a sulfated solid oxide (Examples 3-5) generally had higher Mw's and Mn's as compared to polymers produced using either the fluorided solid oxide alone (Example 1) or the sulfated solid oxide alone (Example 2).

TABLE I Activator-Supports and Polymer Properties of Examples 1-5. Activator- Mn Mw Example Supports (g/mol) (g/mol) 1 100 mg F-Si/Al 109,200 304,700 2 100 mg S-Al 119,000 332,800 3  75 mg F-Si/Al 118,100 324,400  25 mg S-Al 4  50 mg F-Si/Al 120,300 335,700  50 mg S-Al 5  25 mg F-Si/Al 126,500 353,300  75 mg S-Al

Examples 6-10

Examples 6-10 were performed in substantially the same manner as Examples 1-5, except that 2 mg of MET-B were used instead of MET-A, and catalyst productivity or polymer production was within +/−5% of 130 grams for Examples 6-10. Table II summarizes the activator-supports used in Examples 6-10 and the molecular weight properties of the polymers of Examples 6-10 (these homopolymers had melt index values from zero to 0.5 g/10 min).

As shown in Table II, the polymers produced using both a fluorided solid oxide and a sulfated solid oxide (Examples 8-10) unexpectedly had higher Mw's and Mn's as compared to polymers produced using either the fluorided solid oxide alone (Example 6) or the sulfated solid oxide alone (Example 7).

TABLE II Activator-Supports and Polymer Properties of Examples 6-10. Activator- Mn Mw Example Supports (g/mol) (g/mol) 6 100 mg F-Si/Al 75,200 188,900 7 100 mg S-Al 73,900 197,100 8  75 mg F-Si/Al 78,800 199,800  25 mg S-Al 9  50 mg F-Si/Al 85,100 218,200  50 mg S-Al 10  25 mg F-Si/Al 88,300 210,500  75 mg S-Al

The invention is described above with reference to numerous aspects and embodiments, and specific examples. Many variations will suggest themselves to those skilled in the art in light of the above detailed description. All such obvious variations are within the full intended scope of the appended claims. Other embodiments of the invention can include, but are not limited to, the following (embodiments are described as “comprising” but, alternatively, can “consist essentially of” or “consist of”):

Embodiment 1. A catalyst composition comprising a metallocene compound, activator-support I, activator-support II, and an optional co-catalyst, wherein activator-support I comprises a halided solid oxide and activator-support II comprises a sulfated solid oxide and/or a phosphated solid oxide.

Embodiment 2. The composition defined in embodiment 1, wherein the metallocene compound comprises chromium, vanadium, titanium, zirconium, hafnium, or a combination thereof.

Embodiment 3. The composition defined in embodiment 1 or 2, wherein the metallocene compound comprises titanium, zirconium, hafnium, or a combination thereof.

Embodiment 4. The composition defined in any one of the preceding embodiments, wherein the metallocene compound comprises any metallocene compound disclosed herein.

Embodiment 5. The composition defined in any one of embodiments 1-4, wherein the metallocene compound comprises an unbridged zirconium or hafnium based metallocene compound and/or an unbridged zirconium and/or hafnium based dinuclear metallocene compound.

Embodiment 6. The composition defined in any one of embodiments 1-4, wherein the metallocene compound comprises an unbridged zirconium or hafnium based metallocene compound containing two cyclopentadienyl groups, two indenyl groups, or a cyclopentadienyl and an indenyl group.

Embodiment 7. The composition defined in any one of embodiments 1-4, wherein the metallocene compound comprises an unbridged zirconium based metallocene compound containing two cyclopentadienyl groups, two indenyl groups, or a cyclopentadienyl and an indenyl group.

Embodiment 8. The composition defined in any one of embodiments 1-4, wherein the metallocene compound comprises an unbridged zirconium based homodinuclear metallocene compound.

Embodiment 9. The composition defined in any one of embodiments 1-4, wherein the metallocene compound comprises an unbridged hafnium based homodinuclear metallocene compound.

Embodiment 10. The composition defined in any one of embodiments 1-4, wherein the metallocene compound comprises an unbridged zirconium and/or hafnium based heterodinuclear metallocene compound.

Embodiment 11. The composition defined in any one of embodiments 1-4, wherein the metallocene compound comprises a bridged zirconium based metallocene compound with a fluorenyl group, and with no aryl groups on the bridging group.

Embodiment 12. The composition defined in any one of embodiments 1-4, wherein the metallocene compound comprises a bridged zirconium based metallocene compound with a cyclopentadienyl group and a fluorenyl group, and with no aryl groups on the bridging group.

Embodiment 13. The composition defined in any one of embodiments 1-4, wherein the metallocene compound comprises a bridged zirconium or hafnium based metallocene compound with a fluorenyl group, and an aryl group on the bridging group.

Embodiment 14. The composition defined in any one of embodiments 1-4, wherein the metallocene compound comprises a bridged zirconium or hafnium based metallocene compound with a cyclopentadienyl group and fluorenyl group, and an aryl group on the bridging group.

Embodiment 15. The composition defined in any one of embodiments 1-4, wherein the metallocene compound comprises a bridged zirconium based metallocene compound with a fluorenyl group, and an aryl group on the bridging group.

Embodiment 16. The composition defined in any one of embodiments 1-4, wherein the metallocene compound comprises a bridged hafnium based metallocene compound with a fluorenyl group, and an aryl group on the bridging group.

Embodiment 17. The composition defined in any one of embodiments 13-16, wherein the aryl group is a phenyl group.

Embodiment 18. The composition defined in any one of embodiments 1-17, wherein the catalyst composition comprises only one metallocene compound.

Embodiment 19. The composition defined in any one of embodiments 1-17, wherein the catalyst composition comprises two or more metallocene compounds.

Embodiment 20. The composition defined in any one of embodiments 1-17, wherein the catalyst composition comprises two metallocene compounds at any weight ratio disclosed herein, e.g., from about 20:1 to about 1:20, from about 2:1 to about 1:2, etc.

Embodiment 21. The composition defined in any one of embodiments 1-20, wherein the solid oxide comprises any solid oxide disclosed herein, e.g., silica, alumina, silica-alumina, silica-coated alumina, aluminum phosphate, aluminophosphate, heteropolytungstate, titania, zirconia, magnesia, boria, zinc oxide, etc., as well as any mixed oxide thereof or any mixture thereof.

Embodiment 22. The composition defined in any one of embodiments 1-20, wherein the solid oxide comprises alumina, silica-alumina, silica-coated alumina, or any mixture thereof.

Embodiment 23. The composition defined in any one of embodiments 1-22, wherein activator-support I comprises a fluorided solid oxide, a chlorided solid oxide, a bromided solid oxide, an iodided solid oxide, or any combination thereof.

Embodiment 24. The composition defined in any one of embodiments 1-23, wherein activator-support II comprises a sulfated solid oxide.

Embodiment 25. The composition defined in any one of embodiments 1-23, wherein activator-support II comprises a phosphated solid oxide.

Embodiment 26. The composition defined in any one of embodiments 1-23, wherein activator-support I comprises fluorided alumina and/or chlorided alumina and activator-support II comprises sulfated alumina and/or phosphated alumina.

Embodiment 27. The composition defined in any one of embodiments 1-23, wherein activator-support I comprises fluorided silica-alumina and/or chlorided silica-alumina and activator-support II comprises sulfated silica-alumina and/or phosphated silica-alumina.

Embodiment 28. The composition defined in any one of embodiments 1-23, wherein activator-support I comprises fluorided silica-coated alumina and/or chlorided silica-coated alumina and activator-support II comprises sulfated silica-coated alumina and/or phosphated silica-coated alumina.

Embodiment 29. The composition defined in any one of embodiments 1-28, wherein a weight ratio of activator-support I to activator-support II in the catalyst composition is in any range of weight ratios disclosed herein, e.g., from about 1:10 to about 10:1, from about 3:1 to about 1:3, from about 1.5:1 to about 1:1.5, etc.

Embodiment 30. The composition defined in any one of the preceding embodiments, wherein the catalyst composition comprises a co-catalyst, e.g., any co-catalyst disclosed herein.

Embodiment 31. The composition defined in any one of the preceding embodiments, wherein the co-catalyst comprises an aluminoxane compound, an organoboron or organoborate compound, an ionizing ionic compound, an organoaluminum compound, an organozinc compound, an organomagnesium compound, an organolithium compound, or any combination thereof.

Embodiment 32. The composition defined in any one of the preceding embodiments, wherein the co-catalyst comprises any organoaluminum compound disclosed herein.

Embodiment 33. The composition defined in any one of the preceding embodiments, wherein the co-catalyst comprises trimethylaluminum, triethylaluminum, tri-n-propylaluminum, tri-n-butylaluminum, triisobutylaluminum, tri-n-hexylaluminum, tri-n-octylaluminum, diisobutylaluminum hydride, diethylaluminum ethoxide, diethylaluminum chloride, or any combination thereof.

Embodiment 34. The composition defined in any one of embodiments 1-30, wherein the co-catalyst comprises an organoaluminum compound, an organozinc compound, an organomagnesium compound, an organolithium compound, or any combination thereof.

Embodiment 35. The composition defined in any one of embodiments 1-30, wherein the catalyst composition is substantially free of aluminoxane compounds, organoboron or organoborate compounds, ionizing ionic compounds, or combinations thereof.

Embodiment 36. The composition defined in any one of embodiments 1-35, wherein the catalyst composition is produced by a process comprising contacting, in any order, the metallocene compound, activator-support I, and activator-support II.

Embodiment 37. The composition defined in any one of embodiments 1-35, wherein the catalyst composition is produced by a process comprising contacting, in any order, the metallocene compound, activator-support I, activator-support II, and the co-catalyst.

Embodiment 38. An olefin polymerization process, the process comprising contacting the catalyst composition defined in any one of the preceding embodiments with an olefin monomer and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce an olefin polymer.

Embodiment 39. The process defined in embodiment 38, wherein the olefin monomer comprises any olefin monomer disclosed herein, e.g., any C₂-C₂₀ olefin.

Embodiment 40. The process defined in embodiment 38 or 39, wherein the olefin monomer and the optional olefin comonomer independently comprise a C₂-C₂₀ alpha-olefin.

Embodiment 41. The process defined in any one of embodiments 38-40, wherein the olefin monomer comprises ethylene.

Embodiment 42. The process defined in any one of embodiments 38-41, wherein the catalyst composition is contacted with ethylene and an olefin comonomer comprising a C₃-C₁₀ alpha-olefin.

Embodiment 43. The process defined in any one of embodiments 38-42, wherein the catalyst composition is contacted with ethylene and an olefin comonomer comprising 1-butene, 1-hexene, 1-octene, or a mixture thereof.

Embodiment 44. The process defined in any one of embodiments 38-43, wherein the polymerization reactor system comprises a batch reactor, a slurry reactor, a gas-phase reactor, a solution reactor, a high pressure reactor, a tubular reactor, an autoclave reactor, or a combination thereof.

Embodiment 45. The process defined in any one of embodiments 38-44, wherein the polymerization reactor system comprises a slurry reactor, a gas-phase reactor, a solution reactor, or a combination thereof.

Embodiment 46. The process defined in any one of embodiments 38-45, wherein the polymerization reactor system comprises a loop slurry reactor.

Embodiment 47. The process defined in any one of embodiments 38-46, wherein the polymerization reactor system comprises a single reactor.

Embodiment 48. The process defined in any one of embodiments 38-46, wherein the polymerization reactor system comprises 2 reactors.

Embodiment 49. The process defined in any one of embodiments 38-46, wherein the polymerization reactor system comprises more than 2 reactors.

Embodiment 50. The process defined in any one of embodiments 38-49, wherein the olefin polymer comprises any olefin polymer disclosed herein.

Embodiment 51. The process defined in any one of embodiments 38-50, wherein the olefin polymer is an ethylene/1-butene copolymer, an ethylene/1-hexene copolymer, or an ethylene/1-octene copolymer.

Embodiment 52. The process defined in any one of embodiments 38-50, wherein the olefin polymer is an ethylene/1-hexene copolymer.

Embodiment 53. The process defined in any one of embodiments 38-52, wherein the polymerization conditions comprise a polymerization reaction temperature in a range from about 60° C. to about 120° C. and a reaction pressure in a range from about 200 to about 1000 psig (about 1.4 to about 6.9 MPa).

Embodiment 54. The process defined in any one of embodiments 38-53, wherein the polymerization conditions are substantially constant, e.g., for a particular polymer grade.

Embodiment 55. The process defined in any one of embodiments 38-54, wherein a molecular weight parameter (e.g., Mn, Mw) of the olefin polymer produced by the process is greater than the molecular weight parameter of an olefin polymer obtained under the same polymerization conditions without activator-support I in the catalyst composition, and greater than the molecular weight parameter of an olefin polymer obtained under the same polymerization conditions without activator-support II in the catalyst composition.

Embodiment 56. The process defined in embodiment 55, wherein the molecular weight parameter is Mw, and the Mw of the olefin polymer produced by the process is greater by any percentage amount disclosed herein, e.g., at least 1%, at least about 3%, from 1% to about 25%, from about 3% to about 20%, etc.

Embodiment 57. The process defined in embodiment 55, wherein the molecular weight parameter is Mn, and the Mn of the olefin polymer produced by the process is greater by any percentage amount disclosed herein, e.g., at least 1%, at least about 3%, from 1% to about 25%, from about 3% to about 20%, etc.

Embodiment 58. The process defined in any one of embodiments 38-57, wherein no hydrogen is added to the polymerization reactor system.

Embodiment 59. The process defined in any one of embodiments 38-57, wherein hydrogen is added to the polymerization reactor system.

Embodiment 60. The process defined in any one of embodiments 38-59, wherein the number-average molecular weight (Mn) of the olefin polymer produced by the process is in any range disclosed herein, e.g., from about 5,000 to about 150,000 g/mol, from about 5,000 to about 50,000 g/mol, from about 10,000 to about 100,000 g/mol, etc.

Embodiment 61. The process defined in any one of embodiments 38-60, wherein the weight-average molecular weight (Mw) of the olefin polymer produced by the process is in any range disclosed herein, e.g., from about 50,000 to about 700,000 g/mol, from about 75,000 to about 500,000 g/mol, from about 100,000 to about 400,000 g/mol, etc.

Embodiment 62. The process defined in any one of embodiments 38-61, wherein the density of the olefin polymer produced by the process is in any range disclosed herein, e.g., from about 0.89 to about 0.96 g/cm³, from about 0.91 to about 0.95 g/cm³, from about 0.91 to about 0.94 g/cm³, etc.

Embodiment 63. The process defined in any one of embodiments 38-62, wherein the melt index (MI) of the olefin polymer produced by the process is in any range disclosed herein, e.g., from 0 to about 25 g/10 min, from about 0.1 to about 10 g/10 min, from about 0.5 to about 3 g/10 min, etc.

Embodiment 64. An olefin polymer produced by the olefin polymerization process defined in any one of embodiments 38-63.

Embodiment 65. An article comprising the olefin polymer defined in embodiment 64.

Embodiment 66. A method for forming or preparing an article of manufacture comprising an olefin polymer, the method comprising (i) performing the olefin polymerization process defined in any one of embodiments 38-63 to produce the olefin polymer, and (ii) forming the article of manufacture comprising the olefin polymer, e.g., via any technique disclosed herein.

Embodiment 67. The article defined in embodiment 65 or 66, wherein the article is an agricultural film, an automobile part, a bottle, a drum, a fiber or fabric, a food packaging film or container, a food service article, a fuel tank, a geomembrane, a household container, a liner, a molded product, a medical device or material, a pipe, a sheet or tape, or a toy. 

The invention claimed is:
 1. An olefin polymerization process, the process comprising contacting a catalyst composition with an olefin monomer and an optional olefin comonomer in a polymerization reactor system under polymerization conditions to produce an olefin polymer, wherein the catalyst composition comprises a metallocene compound, activator-support I, activator-support II, and an optional co-catalyst, wherein: a weight ratio of activator-support I to activator-support II in the catalyst composition is in a range from about 1:10 to about 10:1; activator-support I comprises a halided solid oxide, and activator-support II comprises a sulfated solid oxide and/or a phosphated solid oxide.
 2. The process of claim 1, wherein the catalyst composition comprises a metallocene compound, a fluorided solid oxide, a sulfated solid oxide, and a co-catalyst.
 3. The process of claim 2, wherein the co-catalyst comprises an aluminoxane compound, an organoboron or organoborate compound, an ionizing ionic compound, an organoaluminum compound, an organozinc compound, an organomagnesium compound, an organolithium compound, or any combination thereof.
 4. The process of claim 2, wherein the co-catalyst comprises an organoaluminum compound, wherein the organoaluminum compound comprises trimethylaluminum, triethylaluminum, tri-n-propylaluminum, tri-n-butylaluminum, triisobutylaluminum, tri-n-hexylaluminum, tri-n-octylaluminum, diisobutylaluminum hydride, diethylaluminum ethoxide, diethylaluminum chloride, or any combination thereof.
 5. The process of claim 1, wherein activator-support II comprises a sulfated solid oxide.
 6. The process of claim 1, wherein activator-support II comprises a phosphated solid oxide.
 7. The process of claim 1, wherein activator-support I comprises fluorided alumina and/or chlorided alumina, and activator-support II comprises sulfated alumina and/or phosphated alumina.
 8. The process of claim 1, wherein activator-support I comprises fluorided silica-alumina and/or chlorided silica-alumina, and activator-support II comprises sulfated silica-alumina and/or phosphated silica-alumina.
 9. The process of claim 1, wherein activator-support I comprises fluorided silica-coated alumina and/or chlorided silica-coated alumina, and activator-support II comprises sulfated silica-coated alumina and/or phosphated silica-coated alumina.
 10. The process of claim 1, wherein the polymerization reactor system comprises a batch reactor, slurry reactor, gas-phase reactor, solution reactor, high pressure reactor, tubular reactor, autoclave reactor, or any combination thereof.
 11. The process of claim 1, wherein a Mw of the olefin polymer produced by the process is greater than a Mw of an olefin polymer obtained under the same polymerization conditions without activator-support I in the catalyst composition, and greater than a Mw of an olefin polymer obtained under the same polymerization conditions without activator-support II in the catalyst composition.
 12. The process of claim 1, wherein a Mn of the olefin polymer produced by the process is greater than a Mn of an olefin polymer obtained under the same polymerization conditions without activator-support I in the catalyst composition, and greater than a Mn of an olefin polymer obtained under the same polymerization conditions without activator-support II in the catalyst composition.
 13. The process of claim 1, wherein the catalyst composition is contacted with ethylene and an olefin comonomer comprising 1-butene, 1-hexene, 1-octene, or a mixture thereof.
 14. The process of claim 13, wherein the ethylene polymer has: a melt index of less than or equal to about 25 g/10 min; a density in a range from about 0.89 g/cm³ to about 0.96 g/cm³; a Mw in a range from about 75,000 to about 500,000 g/mol; and a Mn in a range from about 5,000 to about 150,000 g/mol.
 15. The process of claim 13, wherein the catalyst composition comprises a metallocene compound, a fluorided solid oxide, a sulfated solid oxide, and an organoaluminum compound.
 16. The process of claim 13, wherein the catalyst composition comprises a metallocene compound, a fluorided solid oxide, a phosphated solid oxide, and an organoaluminum compound.
 17. The process of claim 13, wherein the polymerization reactor system comprises a loop slurry reactor.
 18. A catalyst composition comprising a metallocene compound, activator-support I comprising a halided solid oxide, activator-support II comprising a sulfated solid oxide and/or a phosphated solid oxide, and an optional co-catalyst; wherein: a weight ratio of activator-support I to activator-support II is in a range from about 1:10 to about 10:1.
 19. The composition of claim 18, wherein: activator-support I comprises fluorided alumina, fluorided silica-alumina, fluorided silica-coated alumina, or a combination thereof; and activator-support II comprises sulfated alumina, sulfated silica-alumina, sulfated silica-coated alumina, or a combination thereof.
 20. The composition of claim 18, wherein the catalyst composition comprises a metallocene compound, a fluorided solid oxide, a sulfated solid oxide, and a co-catalyst.
 21. The composition of claim 20, wherein the metallocene compound comprises an unbridged zirconium or hafnium based metallocene compound containing two cyclopentadienyl groups, two indenyl groups, or a cyclopentadienyl and an indenyl group.
 22. The composition of claim 20, wherein the metallocene compound comprises a bridged zirconium or hafnium based metallocene compound with a cyclopentadienyl group and fluorenyl group.
 23. The composition of claim 20, wherein the co-catalyst comprises an aluminoxane compound, an organoboron or organoborate compound, an ionizing ionic compound, an organoaluminum compound, an organozinc compound, an organomagnesium compound, an organolithium compound, or any combination thereof.
 24. The composition of claim 20, wherein the co-catalyst comprises an organoaluminum compound.
 25. The process of claim 13, wherein the polymerization reactor system comprises a slurry reactor, a gas-phase reactor, a solution reactor, or a combination thereof.
 26. The process of claim 13, wherein the catalyst composition comprises: a metallocene compound; activator-support I comprising fluorided alumina, fluorided silica-alumina, fluorided silica-coated alumina, or a combination thereof; activator-support II comprising sulfated alumina, sulfated silica-alumina, sulfated silica-coated alumina, or a combination thereof; and an organoaluminum co-catalyst.
 27. The process of claim 26, wherein a Mw of the olefin polymer produced by the process is greater than a Mw of an olefin polymer obtained under the same polymerization conditions without activator-support I in the catalyst composition, and greater than a Mw of an olefin polymer obtained under the same polymerization conditions without activator-support II in the catalyst composition.
 28. The process of claim 26, wherein a Mn of the olefin polymer produced by the process is greater than a Mn of an olefin polymer obtained under the same polymerization conditions without activator-support I in the catalyst composition, and greater than a Mn of an olefin polymer obtained under the same polymerization conditions without activator-support II in the catalyst composition.
 29. The process of claim 26, wherein the metallocene compound comprises an unbridged zirconium or hafnium based metallocene compound containing two cyclopentadienyl groups, two indenyl groups, or a cyclopentadienyl and an indenyl group.
 30. The process of claim 26, wherein the metallocene compound comprises a bridged zirconium or hafnium based metallocene compound with a cyclopentadienyl group and fluorenyl group. 